Crude Oil Emulsions - Petroleum Engineers Handbook.pdf

Chapter 19

Crude Oil Emulsions H. Vernon Smith, Kenneth E. Arnold,

Meridian

Corp.

Paragon Engineermg Scr~icm Inc.

Introduction

Theories of Emulsions

Much of the oil produced worldwide is accompanied by water in an emulsion that requires treating. Even in those fields where there is essentially no initial water production. water cuts may increase in time to the point where it is necessary to treat the emulsion. Water content of the untreated oil may vary from a fraction of I % to over 90%. To prevent increased transportation costs, water treatment and disposal costs, and deterioration of equipment, purchasers of crude oil limit the basic sediment and water (BSSCW) content of the oil they purchase. Limits vary depending on local conditions, practices. and contractual agreements and typically range from 0.2 to 3.0%. BY&W is usually predominantly water but may contain solids. The solids contained in the BS&W come from the producing formation and consist of sand. silt, mud, scale. and precipitates of dissolved solids. These troublesome solids vary widely from producing field to field. zone to zone, and well to well. Purchasers may also limit the salt content of the oil. Removing water from the stream decreases the salt content. Salt content along with BS&W are the two importsnt crude purchasing requirements. When water forms a stable emulsion with crude oil and cannot be removed in conventional storage tanks. emulsion-treating methods must be used. The methods. procedures, equipment, and systems generally used in treating crude oil emulsions are considered in this chapter, Space limitation does not permit the rigorous trcatment of crude oil emulsions. Many topics and sub-topics exist on which entire chapters can be written. This chaptcr contains an abbreviated discussion of only a few of the most important and pertinent considerations of crude oil emulsions. More detailed and diversified discussions on crude oil emulsions can be found in the General References at the end of the chapter.

An emulsion is a heterogeneous liquid system consisting of two immiscible liquids with one of the liquids intimately dispersed in the form of droplets in the second liquid. An emulsion is distinguished from a simple dispersion of one liquid in another by the fact that, in an emulsion, the probability of coalescence of droplets on contact with one another is greatly reduced because of the presence of an emulsifier, which inhibits coalescence. Such inhibition is not present in a dispersion. The stability of the emulsion is controlled by the type and amount of surface-active agents and/or finely divided solids. which commonly act as emulsifying agents or emulsifiers. As shown in Fig. 19.1, these emulsifying agents form interfacial films around the droplets of the dispersed phase and create a barrier that slows down or prevents coalescence of the droplets. The matrix of an emulsion is called the external or continuous phase. The portion of the emulsion that is in the form of small droplets is called the internal, dispersed, or discontinuous phase. The emulsions considered in this chapter consist of crude oil and water or brine produced with it. In most emulsions of crude oil and water, the water is finely dispersed in the oil. The spherical form of the water globules is a result of interfacial tension (IFT). which compels them to present the smallest possible surface area to the oil. This is a water-in-oil emulsion and is referred to as a “normal” emulsion. The oil can be dispersed in the water to form an oil-in-water emulsion, which is referred to as an “inverse” or “reverse” emulsion. A typical reverse emulsion is shown in Fig. 19.2. Emulsions are sometimes interrelated in a more complex form. The emulsion may be either water-in-oil or oil-in-water to begin with, but additional agitation may

Definition

of an Emulsion

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Fig. 19.1—Photomicrograph of water-in-oil emulsion. Observe the riqid-appearing film or skin that retards coalescence.

Fig. 19.2—Photomicrograph of reverse emulsion. Uniformly sized oil particles are about 10 µm in diameter and are dispersed in the continuous water phase.

cause it to become multistage. If it is a water-in-oil emulsion initially, a water-in-oil-in-water emulsion can be formed if a small volume of the original water-in-oil emulsion is enveloped in a film of water. It is also possible to form multistage emulsions in an oil continuous phase as shown in Figs. 19.3 and 19.4. This alternating externalphase/internal-phase/external-phase arrangement has been known to exist in eight stages. Multistage emulsions usually add appreciably to the problem of separating the emulsion into oil and water. The more violent the agitation, the more likely multistage emulsions are to form.

found in areas of Canada, California, Venezuela, and other areas. Oil-in-water emulsions are generally resolved in the same way as water-in-oil emulsions, except electrostatic treaters cannot be used on oil-in-water emulsions. The agitation necessary to form an emulsion may result from any one or a combination of several sources: (1) the bottomhole pump, (2) flow through the tubing, wellhead, manifold, or flowlines, (3) the surface transfer pump, or (4) pressure drop through chokes, valves, or other surface equipment. The greater the amount of agitation, the smaller the droplets of water dispersed in the oil. Figs. 19.5 through 19.9 show common crude oil emulsions that demonstrate the range of droplet sizes normally encountered. Studies of water-in-oil emulsions have shown that water droplets are of widely varying sizes, ranging from less than 1 to about 1,000 µm. Emulsions that have smaller droplets of water are usually more stable and difficult to treat than those that have larger droplets. Crude oils vary widely in their emulsifying tendencies. Some may form very stable emulsions that are difficult to separate, while others may not emulsify or may form a loose emulsion that will separate quickly. The presence, amount, and nature of an emulsifying agent determines whether an emulsion will be formed and the stability of that emulsion. If the crude oil and water contain no emulsifying agent, the oil and water may form a dispersion that will separate quickly because of rapid coalescence of the dispersed droplets. On the other hand, if an emulsifying agent is present in the crude oil, a very stable emulsion can be formed.

How Crude Oil Emulsions Form The three conditions necessary for the formation of an emulsion are (1) the two liquids forming the emulsion must be immiscible, (2) there must be sufficient agitation to disperse one liquid as droplets in the other, and (3) there must be an emulsifying agent present. Crude oil and water are immiscible. If gently poured into the same container, they will quickly separate. If the oil and water are violently agitated, small drops of water will be dispersed in the continuous oil phase and small drops of oil will be dispersed in the continuous water phase. If left undisturbed, the oil and water will quickly separate into layers of oil and water. If any emulsion is formed, it will be between the oil above and the water below. When considering crude oil emulsions, we are usually concerned with water-in-oil emulsions because most emulsions are this type. Oil-in-water emulsions are encountered in some heavy oil production, however, such as that

CRUDE OIL EMULSIONS

Fig. 19.3—Photomicrograph of oil-in-water-in-oil emulsion. Oil droplets are shown dispersed in water droplets that are dispersed in the continuous oil phase.

19-3

Fig. 19.4—Photomicrograph of multiple-stage emulsion from Rocky Mountain field. The dispersed water phase contains small oil particles.

If an emulsion is not treated, a certain amount of water will separate from the oil by natural coalescence and settling because of the difference in density of oil and water. Unless some form of treatment is used to accomplish complete separation, however, there probably will be a small percentage of water left in the oil even after extended settling. The water that remains in the oil will be in minute droplets that have extremely slow settling velocities. They will be widely dispersed so that there will be little chance for them to collide, coalesce into larger droplets, and settle. The amount of water that emulsifies with crude oil in most production systems may vary from less than 1 to more than 60% in rare cases. The most common range of emulsified water in light crude oil-i.e., oil above 20° API-is from 5 to 20 vol%. The most common range of emulsified water in crude oil heavier than 20° API is from 10. to 35%. Emulsifying Agents Emulsifying agents are surface-active compounds that attach to the water-drop surface and lower the oil/water IFT. When energy is added to the mixture by agitation, the dispersed-phase droplets are broken into smaller droplets. The lower the IFT, the smaller the energy input required for emulsification-i.e., with a given amount of agitation, smaller droplets will form. There are many theories on the nature of emulsifying agents in crude oil emulsions. Some emulsifiers are thought to be asphaltic in nature. They are barely soluble

Fig. 19.5—Photomicrograph of loose emulsion from western Kansas containing about 30% emulsified water in the form of droplets ranging in diameter from about 60 µm downward.

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Fig. 19.6—Photomicrograph of water-in-oil emulsion with dispersed particles of water ranging in size from about 250 to about 1 µm.

Fig. 19.8—Photomicrograph of tight emulsion with the dispersed water particles varying in size from 1 to 20 µm.

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Fig. 19.7—Photomicrograph of relatively tight water-in-oil emulsion. Largest water droplets are about 60 µm, medium droplets are about 40 µm, and the smallest ones are about 1 to 20 µm.

in oil and are strongly attracted to the water. They come out of solution and attach themselves to the droplets of water as these droplets are dispersed in the oil. They form thick films that surround the water droplets and prevent the surfaces of the water droplets from contacting, thus preventing coalescence when the droplets collide. Oil-wet solids-such as sand, silt, shale particles, crystallized paraffin, iron, zinc, aluminum sulfate, calcium carbonate, iron sulfide, and similar materials-that collect at the oil/water interface can act as emulsifiers. Fig. 19.10 shows some of these solids removed from a crude oil emulsion. These substances usually originate in the oil formation but can be formed as the result of an ineffective corrosion-inhibition program. Many emulsions are prepared for commercial use. An emulsion of kerosene and water is used for spraying fruit trees; soap is used as the emulsifying agent. Eggs supply the emulsifying agent used in the preparation of mayonnaise from vegetable oil and vinegar: These are very stable emulsions. Most but not all crude oil emulsions are dynamic and transitory. The interfacial energy per unit of area in petroleum emulsions is rather high compared with familiar industrial emulsions. They are therefore thermodynamically unstable in the sense that if the dispersed water coalesced and separated, the total free energy would decrease. Only the presence of an emulsifier film introduces an energy barrier that prevents the “breaking” or separation process from proceeding. The characteristics of an emulsion change continually from the time of formation to the instant of complete resolution. This occurs because there are numerous types of

CRUDE OIL EMULSIONS

Fig. 19.9—Photomicrograph of tight emulsion from Huntington Beach, CA; water content 20%, with the average water droplet diameter less than 5 µm.

adsorbable materials in a given oil. Also, the adsorption rate of the emulsion and permanence of location at the interface may vary as the fluid flows through the process. Furthermore, the emulsion characteristics are changed as the liquid is subjected to changes in temperature, pressure, and degree of agitation. Prevention of Emulsions If all water can be excluded from the oil as it is produced and/or if all agitation of well fluids can be prevented, no emulsion will form. Exclusion of water in some wells is difficult or impossible, and the prevention of agitation is almost impossible. Therefore, production of emulsion from many wells must be expected. In some instances, however, emulsification is increased by poor operating practices. Operating practices that include the production of excess water as a result of poor cementing or reservoir management can increase emulsion-treating problems. In addition, a process design that subjects the oil/water mixture to excess turbulence can result in greater treating problems. Unnecessary turbulence can be caused by overpumping and poor maintenance of plunger and valves in rod-pumped wells, use of more gas-lift gas than is needed, and pumping the fluid where gravity flow could be used. Some operators use progressive cavity pumps as opposed to reciprocating, gear, or centrifugal pumps to minimize turbulence. Others have found that some centrifugal pumps can actually cause coalescence if they are installed

Fig. 19.10—Photomicrograph showing a collection of inorganic solids removed from an emulsion by filtering and washing. These solids include calcite, silica, iron compounds, obsidian, and black carbonaceous materials.

in the process without a downstream throttling valve. Wherever possible, pressure drop through chokes and control valves should be minimized before oil/water separation. Color of Emulsions The color of a crude oil emulsion can vary widely, depending on the oil and water content of the emulsion and the characteristics of the oil and water. The most common color of emulsions is a dark reddish brown. However, any color from light green or yellow to grey or black may be found. “Brightness” is an indicator of the presence of an emulsion. Oil-free water and water-free oil are clear and bright. Emulsions are murky and opaque because of reflection and scattering/of light at the oil/water interfaces of the dispersed phase. The greater the total interfacial area between the oil and water, the lighter the color of the emulsion. That is, an emulsion containing many small droplets of water will tend to be lighter than one containing an equal volume of water in larger droplets because the latter has less total interfacial surface area. Stability of Emulsions Generally, crude oils with low API gravity (high density) will form a more stable and higher-percentage volume of emulsion than will oils of high API gravity (low density). Asphaltic-based oils have a tendency to emulsify more readily than paraffin-based oils. High-viscosity crude oil

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19-6

will usually form a more stable emulsion than lowviscosity oil. Emulsions of high-viscosity crude oil usually are very stable and difficult to treat because the viscosity of the oil hinders or prevents movement of the dispersed water droplets and thus retards their coalescence. In addition, high-viscosity/high-density oils usually contain more emulsifiers than lighter oils.

Effect of Emulsion

on Viscosity of Fluids

Emulsions are always more viscous than the clean oil contained in the emulsion. The ratio of the viscosity of an emulsion to the viscosity of the clean crude oil in oilfield emulsions depends on the shear rate to which it has been subjected. The authors have found that for many emulsions and the shear rates normally encountered in piping systems, this shear rate can be approximated by the following equation if no other data are available.

~,/~~~=1+2.5f+l4.lJ”,

. .....

. . . (1)

where cce = viscosity of emulsion. PO = viscosity of clean oil, and f = fraction of the dispersed phase.

Sampling and Analyzing Crude Oil Emulsions Purchasers of crude oil have established certain specifications that must be met before they will accept oil from a producer. These specifications limit the amount of BS&W in the oil. The limitations are usually strict, and if the amount of ES&W in the oil exceeds the specified limit. the oil may not be accepted by the purchaser. The seller and buyer must agree on the procedure for sampling and analyzing the oil to provide consistent and mutually acceptable data. The performance of emulsion-treating units or systems can be observed and studied by the practice of regularly and periodically withdrawing and analyzing samples of the contents at multiple levels in the vessels or multiple points in the systems. This is particularly beneficial in treating emulsions involving viscous oils. Samples of emulsions should be representative of the liquid from which they are taken. Emulsification should not occur when the sample is extracted. Samples obtained at the wellhead. manifold, or oil and gas separator may show a high percentage of emulsion, but the oil and water in the system may actually not be emulsified. This indicates that emulsification occurred because of the turbulence created as the sample was removed from the pressure zone to the sample container. It is possible to take a sample from a pressure zone without further emulsification of the liquids if the velocity of the discharging liquid is controlled. One method is to use a piece of small-diameter tubing approximately 10 to 15 ft.long. One end of the tubing is connected to a bleeder valve on the line or vessel from which the sample is to be extracted, and the other end is connected to the sample container. The bleeder valve should be opened fully and the sample allowed to flow through the smalldiameter tubing into the container. The pressure drop from

HANDBOOK

the line to the container is absorbed by flow through the tubing. Flow through the tubing, however, can cause either coalescence or additional emulsification. Another method of withdrawing a representative sample of emulsion is to use a sample container initially filled with water. The sample container is equipped with valves at the top and bottom with the top valve connected to the point from which the sample is to be extracted. The top valve of the container is opened first and the container pressured from the line. The valve at the bottom of the container is then opened and the water discharged into the atmosphere as the sample enters the container. There will be no emulsification in the container because there is no pressure drop between the source and sample container to cause turbulence. Once the sample is taken, pressure can be bled off through a third valve with little effect on the sample. Small centrifuges are used to determine BS&W content of crude oil. The centrifuges may be driven by hand or electric motor. A small measured volume of sample is diluted with solvent and placed in graduated glass containers. These are then inserted into the centrifuge and rotated at high speed for a few minutes. Separation of the oil, water, and solids is accomplished by centrifugal force. The percentages of each constituent can be read directly from the graduated containers in which the sample is centrifuged. The speed used in these small centrifuges varies from 2,000 to 4,000 revimin. Methods of taking and analyzing samples of crude oil for custody transfer are included in the API Mur~uul of Petroleum Measurement Standards. Also see Chap. 17.

Methods Used in Treating Crude Oil Emulsions Three basic steps usually are required to separate a crudeoil/water emulsion into bulk phases of oil and water. Step l-Destabilization. An emulsion is destabilized by counteracting the stabilizing effect of the emulsifier. The tough skin or film surrounding the dispersed water droplets must be weakened and broken. This is usually accomplished by adding heat and/or a properly selected, interfacially active chemical compound to the emulsion. Step 2-Coalescence. After the films encasing the dispersed droplets are broken, the dispersed droplets must coalesce into drops large enough to settle out of the continuous phase of oil. Fig. 19.11 shows a small droplet of water breaking through a destabilized emulsion film to coalesce with the bigger drop. This usually is accomplished by imposing a period of moderate agitation or by subjecting the destabilized emulsion to an alternating electric field. This will increase the dispersed droplets contacting rate. Thus coalescence will increase, resulting in larger droplets. Step 3-Gravity Separation. A quiet period of settling must be provided to allow the coalesced drops to settle out of the oil because of the difference in density between the water and oil. This is accomplished by providing a sufficient residence time and a favorable flow pattern in a tank or vessel that will allow the coalesced drops of water to separate from the oil. Another way of stating the general emulsion-treating procedure is that to resolve a crude-oil/water emulsion into bulk oil and water three things must be done:

CRUDE OIL EMULSIONS

19-7

TABLE 19.1-METHODS COALESCENCE,

TO AID DESTABILIZATION, AND/OR SETTLING

Destabilization Chemical Heating Coalescence Agitation Coalescing plates Electric field Water washing Filtering Fibrous packing Heating Retention time Centrifugation Gravity Separation Gravity settling Heating Centrifugation

other temperatures by drawing a straight line parallel to the others. If the viscosity is unknown at any temperature, the lines on the chart may be used. API Spec. l2L recommends that crude be heated so that its viscosity is below 150 SSV (about 50 cSt) for treating.

Fig. 19.11 -A waler-in-oil emulsion with the film or skin surrounding the water droplet in the process 01 rupturing.

(I) increase the probability of coalescence of dispersed water droplets on contact, (2) make the rate of contact of dispersed water droplets high without creating high shear forces, and then (3) allow the liquids to settle quietly so that they can separate into bulk phases of oil and water. All the incidental variables, such as selection of proper chemical, rate of chemical injection, treating temperature and pressure, oil and emulsion viscosity, flow rate, vessel design, vessel size, and fluid levels, are controlled to execute these three steps in the quickest and most economical manner. An emulsion-treating unit or system will use one or more of the methods in Table 19. I to aid in destabilizing, coalescence, and/or settling. Each of these treating methods that can be used to resolve an emulsion is discussed separately.

Heating The use of heat in treating crude oil emulsions has four basic benefits. I. Heat reduces the viscosity of the oil, resulting in a greater force during collision of the water droplets. Also, the reduced oil viscosity allows the water droplets to settle more rapidly through the less viscous oil, Fig. 19.12 can be used to estimate crude oil viscosity/temperature relationships. Viscosities vary widely from one crude to another. The curves should be used only in the absence of specific data. If the viscosity of the crude is known at two temperatures, the viscosity at other temperatures can be approximated by a straight line. If the viscosity is known at one temperature, it can be approximated at

2. Heat increases the droplets’ molecular movement. This aids in coalescence through increased collision frequency of the dispersed-phase droplets. 3. Heat may deactivate the emulsifier (e.g., dissolving paraffin crystals) or it can enhance the action of treating chemicals, causing the chemical to work faster and more thoroughly to break the film surrounding the droplets of the dispersed phase of the emulsion. 4. Heat may also increase the difference in density between the oil and the water, thus accelerating settling. In general, at temperatures below 180”F, the addition of heat will increase the difference in density. Most light oils are treated below 180°F; thus the effect of heat on gravity is beneficial. For heavy crudes (below 20”API). which normally are treated above 180”F, heat may have a negative effect on difference in density. In special cases, increased heat may cause the density of water to be less than that of oil. This effect is shown in Fig. 19.13. Heating well fluids is expensive. Adding heat can cause a significant loss of the lower-boiling-point hydrocarbons (light ends). This results in “shrinkage” of the oil, or loss of volume. Because the light ends are boiled off, the remaining liquid has a lower API gravity and thus may have a lower value. Figs. 19. I4 and 19.15 illustrate typical gravity and volume losses for 33”API crude vs. temperature. The molecules leaving the oil phase may be vented or compressed and sold with the gas. Even if they are sold with the gas, there probably will be a net loss in income. The gas liberated when crude oil is treated may also create a problem in the treating equipment if the equipment is not properly designed. In vertical emulsion treaters and gun barrels, some gas may rise through the coalescing section. The liberated gas can create enough turbulence and disturbance to inhibit coalescence. Perhaps more important, the small gas bubbles have an attraction for surface-active material and hence for the water droplets; thus they have a tendency to keep the water droplets from settling and even may cause them to be discharged with the oil.

19-8

Fig. 19.12-Approximate

1 0

*oo

200

viscosity/temperature

300

Temperature.DF Water

Crude C

0

100 200 Temperature. DF

300

Fig. 19.13--Relationship of specific gravity with temperature for three crude oils.

relationships for crude oil

Fuel is required to provide heat, and the cost of fuel must be considered. If the oil is much above ambient temperature when discharged from the treating unit, it can be flowed through a heat exchanger with the incoming well fluid to transfer the heat to the cooler incoming well fluid. This will minimize evaporation losses and reduce fuel cost. It will also increase the vapor pressure of the crude, however, which may be limited by contract. If properly applied, heating an emulsion can have great beneficial effect on water separation. The most economical emulsion treating may be obtained by use of less heat and a little more chemical, agitation, and/or settling space. In some geographic areas, emulsion heating requirements vary in accordance with daily and/or seasonal atmospheric temperatures. Emulsions are usually more difficult to treat when it is cool-at night, during a rain, or in winter months when the atmospheric temperatures are lowest. Treatment, especially heating, may not be required in warmer summer months. Where the treating problem is seasonal, some emulsions can be resolved successtilly by addition of more chemical demulsifiers during winter months. Study is required to determine the proper economic balance of heat and chemicals. Crude oil emulsions with similar viscosity ranges do not always require the same type of treating equipment or the same treating temperature. Emulsions produced

CRUDE OIL EMULSIONS

19-9

TYPICAL

33’

GRAVITY

API

LOSS

50 TEMPERATURE,

Fig. 19.14-API

from different wells on the same lease or from the same formation in the same field may require different treating temperatures. For this reason, it is recommended that low treating temperatures be tested so that the lowest practical treating temperature for each emulsion and treating unit or system can be determined by trial. The heat input and thus the fuel required for treating depends on the temperature rise, amount of water in the oil, and the flow rate. It requires about twice as much energy to heat a given volume of water as it does to heat the same volume of oil. For this reason, it is beneficial to separate free water from the emulsion to be treated. Often this is accomplished in a separate free-water knockout vessel upstream of the point where heat is added. Sometimes it is accomplished in a separate section of the same vessel.

The required heat input for an insulated vessel (heat loss is assumed to be 10% of heat input) can be approximated from

+q,,,yb,,),

(2)

where

Q = heat input, Btu/hr. in temperature, “F, 90 = oil flow rate, B/D, 9 1, = water flow rate, B/D, Yo = specific gravity of oil, and Yn = specific gravity of water.

AT = increase

Chemical

80 TEMPERATURE,

gravity loss vs. temperature for crude oil.

Q= 16AT(OSy,y,

70

‘F

Demulsifiers

Certain chemical compounds are widely used to destabilize and to assist in coalescence of crude oil emulsions. These are referred to as dehydration chemicals or demulsifiers. This treatment method is popular because the

Fig. 19.15-Percent

110

130

150

lF

loss by volume vs. temperature for crude oil.

chemicals are easily applied to the emulsion, usually are reasonable in cost, and usually minimize the amount of heat and settling time required. The chemical counteracts the emulsifying agent, allowing the dispersed droplets of the emulsion to coalesce into larger drops and settle out of the matrix. For demulsifiers to work, they must (1) be injected into the emulsion, (2) intimately mix with the emulsion and migrate to all of the protective films surrounding all of the dispersed droplets, and (3) displace or nullify the effect of the emulsifying agent at the interface. A period of continued moderate agitation of the treated emulsion to produce contact between and coalescence of the dispersed droplets and a quiet settling period must exist to allow separation of the oil and water. Four actions are required of a chemical demulsifier. Strong attraction to the oil/warer interjace. The demulsifier must have ability to migrate rapidly through the oil phase to reach the droplet interface where it must counteract the emulsifying agent. Flocculation. The demulsifier must have an attraction for water droplets with a similar charge and bring them together. In this way, large clusters of water droplets gather, which look like bunches of fish eggs under a microscope. Coalescence. After flocculation, the emulsifier film is still continuous. If the emulsifier is weak, the flocculation force may be enough to cause coalescence. This is not true in most cases, and the demulsifier must therefore neutralize the emulsifier and promote rupture of the droplet interface film. This allows coalescence to occur. With the emulsion in a flocculated condition, the film rupture results in growth of water drop size. Solids Wetting. Iron sulfides, clays, and drilling muds can be made water-wet, causing them to leave the interface and be diffused into the water droplets. Paraffins and

19-10

asphaltenes can be dissolved or altered by the demulsitier to make their films less viscous, or they can be made oilwet so that they will be dispersed in the oil. The demulsifier selection should be made with all functions of the treating system in mind. If the process is a settling tank, a relatively slow-acting demulsifier can be applied with good results. On the other hand, if the system is an electrostatic process, where some of the flocculation and coalescing action is accomplished by the electric field, there is need for a quick-acting demulsifier. Time for demulsifier action in a vertical emulsion treater normally will be somewhere between that of a settling tank and that of an electrostatic treater. As field conditions change and/or the treating process is modified, the chemical requirements may change. Seasonal changes may cause paraffin-induced emulsion problems. Well workovers may change solids content, which may alter emulsion stability. So no matter how satisfactory a demulsifier is, it cannot be assumed that it will always be satisfactory over the life of the field. While the first commercial emulsion-treating chemical was a solution of soap, present-day chemicals are based on highly sophisticated materials. Chemical emulsion breakers are complex organic compounds with surfaceactive characteristics. The active properties may be derived from any one or a combination of nonionic, cationic, and anionic materials. Within each of these types, compositions are used that will confer various degrees of hydrophobeihydrophile balance to the chemical as desired. The active components are highly viscous and sometimes even solids. It is necessary to use a carrier that will make handling easier: this carrier is almost without exception an organic solvent. Solvent systems are designed to make emulsion breakers compatible with the crude oil system in which they are used. It is also necessary to omit materials that will interfere with refining processes, such as those that will poison catalysts. Therefore, no organic chlorides, bromides, iodides, fluorides, or compounds of arsenic or lead are used in the manufacture of most emulsion-treating chemicals. There is no simple designation of specific chemicals to treat specific emulsions. There are, however, certain common demulsifier types that tend to produce a consistent reaction in many water-in-oil emulsions. Some of the demulsifier types are as follows. Pol~~lvcc~lesters are characterized by quick brightening of emulsjons. but frequently tend toward slow water drop and sludging; they are subject to overtreating problems. Lo~r,-lnolrculrrr-~~‘~~i~~~t resin derivatives tend toward rapid water drop and fair to good overall demulsification properties; they show some tendency toward overtreatment in high-API-gravity emulsions. High-molecular-weight resin derivatives generally have a strong wetting tendency and fair brightening and waterdrop characteristics; they are always used in combination with other materials. Sulfonates exhibit fair to good wetting and water-drop performance, some ability to brighten oil, and very little tendency to overtreat, particularly in high-gravity emulsions. Polymerized oils and esters produce specific characteristics on particular emulsions; they are generally poor for widespread application and are always used in combination with other materials.

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Alkanolamine condensates promote water drop in some emulsions and may produce some brightening; they are blended with other materials for overall good performance. Oxyalkylatedphenols are predominantly wetting agents with fair to poor demulsification properties; they are used in blending to improve demulsifier performance. Polyamine derivatives produce good brightening characteristics and are good blending agents; they are relatively poor in other respects. There are many specific variations within each of these broad categories. Most demulsifiers used in breaking crude oil emulsions are blends of the above and other compounds. The components selected for a given demulsifier are chosen to provide the necessary actions to achieve complete emulsion treatment. The number of different surface-active materials that can act as emulsifiers in crude oil is large. The possible combinations of these emulsifying agents is almost infinite. Therefore, the number of demulsifiers and their combinations must likewise be numerous to treat the emulsions. The type and composition of the crude oil in the emulsion being treated has more influence on how a certain chemical demulsifier will perform than does the specific category of components included in the treating chemical. For example, a low-molecular-weight resin used in treating an emulsion of 35”API oil may exhibit rapid water drop, but that same chemical, when used in treating an emulsion of I5”API oil, may not cause rapid water drop. This illustrates that demulsifying chemicals must be compounded for each particular emulsion. Each treating system must be tested and checked to ensure that the chemicals used for treating the water for disposal do not conflict with chemicals used for treating the oil emulsion. One chemical must not react with the other to cause problems, such as stabilizing the oil in the water. Compatibility of the two chemicals must be tested by bottle tests and then by field tests in the actual treating system. Also, compatibility tests should be performed for any other chemicals added to the produced fluids. Selection of the optimum chemical to use usually starts with bottle tests. A representative sample of fluid is taken and transferred into several test bottles. Several demulsifying chemicals are added to the test bottles in various amounts to determine which chemical will best break the emulsion. Additional tests are made to determine the optimum ratio of chemical to fluid. Several series of tests may be necessary at various ratios and temperatures before a selection can be made. Many factors-such as the color and appearance of the oil, clarity of the water, interface quality, required operating temperature, settling time, and BS&W content-are observed during these bottle tests. Bottle tests can be made with the samples of emulsion taken at the wellhead. anywhere in the flowline, at the manifold, or at the entrance to the treating system or tank. Well-equipped mobile laboratories are available, so this type of work can be done in the field. These mobile units should be operated by trained technicians who can minimize testing and optimize selection of chemical demulsifiers. After the bottle tests are made and the best two or three chemicals have been selected, they should be field tested in the treating system to verify that the best chemicals have been selected. Tests should be made in the treating sys-

CRUDE OIL EMULSIONS

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CHEMICAL %-IN. COUPLING DOUGHNUTMADEOF

DOUGHNUT. AREA OF 6 HOLES TO BE LESS THAN CSA OF %-IN. PIPE AREA %-IN. PIPE=O.19635

SQ IN

HOLE A TO BE DRILLED

D=0.177

8 HOLES FOR CHEMICAL DRILLED ON UPSTREAM FACE OF DOUGHNUT

Fig. 19.16-Chemical

IN.

USE %-IN. HOLE (0.156) HOLES ON FAR SIDE

distributor for flowlines 10 in. and larger

tern at various concentrations, operating temperatures, settling times, degrees of mixing, etc., before the final selection is made on the basis of performance and cost. The optimum chemical is one that will provide the clearest, cleanest separation of water from oil at the lowest temperature in the shortest time at the lowest cost per barrel treated and that will not interfere with subsequent deoiling of the water. The required concentration of demulsifying chemical may be as high as 8 gal/l,000 bbl (about 200 ppm) or as low as 1 ga1/5,000 bbl (about 5 .O ppm). This is a range of 40 to 1. The most common range of chemical injection is between 10 and 60 ppm. Application of heat to an emulsion after a demulsifier has been mixed with it increases effectiveness of the chemical by reducing the viscosity of the emulsion and facilitating more intimate mixing of chemical with emulsion. Chemical reaction at the oil/water interface takes place at a more rapid rate at higher temperatures. The point of injection of demulsifier chemical into the emulsion is important. The chemical should be injected into the emulsion and mixed with it so that it is evenly and intimately distributed throughout the emulsion when it is heated, coalesced, and settled in the treating system. The demulsifying chemical should be injected in a continuous stream, with the chemical volume directly proportional to the emulsion volume. Certain demulsifiers should not be present in the emulsion during excessively prolonged agitation because the beneficial effect of the demulsifier may be spent or counteracted by the agitation and re-emulsification may occur. Turbulence accelerates the diffusion of the demulsifier throughout the emulsion and increases the number and intensity of impacts between water droplets. Turbulence must be prolonged for a sufficient time to permit the chemical to reach the interface between the oil and all the dispersed water droplets, but the intensity and duration of the turbulence must be controlled so that it will not cause further emulsification. Turbulence is the dynamic factor that disperses the water in the oil and is a prerequisite

to emulsion formation. A moderate level of controlled turbulence, however, causes the dispersed droplets to collide and coalesce. Usually, this turbulence is provided by normal flow in surface lines, manifolds, and separators and by flow through the emulsion-treating unit or system. One way of assisting in dispersing the chemical throughout the entire volume of emulsion is to mix a small volume of chemical with a diluenr and then to inject and mix the diluted chemical with the emulsion. The larger volume of the mixture may make it possible for the chemical to be more uniformly and intimately mixed with the emulsion. When flow rates are low (less than 3 ft/sec) or when laminar flow is encountered, the injection of chemical into a coupling welded in the side of the pipe is not recommended. In such cases, an injection quill (which injects the chemical in the stream at a location removed from the wall), a chemical distributor (Fig. 19.16), and/or a kinetic mixer (Fig. 19.17) is recommended. The kinetic mixer consists of a series of staggered, helically convoluted vanes that use the velocity of the fluid to accomplish mixing. When a tank of wet oil (oil containing more than the permissible amount of water) accumulates, the tank contents can be treated by adding a small proportion of demulsifier, agitating or circulating the tank contents, and then allowing time for the water to settle in the tank. Trailermounted units that include a heater, circulating pump, and chemical injector are sometimes used for this method of tank treating. This batch-treatment method normally is used as an emergency measure. Excessive amounts of treating chemical can result in increased stability of the water-in-oil emulsion or of the oil-in-water emulsion in the produced water, increase the stability or the volume of the interfacial emulsion and/or sludge, or waste money equal to the cost of the excessive volume of chemical over the optimum volume. Also, the cost of handling and injecting the excessive amount of chemical must be considered along with the purchase cost of the chemical. Insufficient treating chemical can fail to

PETROLEUM ENGINEERING HANDBOOK

A T M O S . VENT

OIL OUT

4

I:=

13 WATER OUT

WATER IN

S.P.PACK TANK INSTALLATION

FREE-FLOW

COALESCENCE

Fig. 19.17—Kinetic (static) mixer for mixing chemical demulsifier with emulsion.

Fig. 19.18—The S. P. Pack’” grows a larger drop size on the inlet separator of a gravity settler.

break the emulsion; allow a quick buildup of excessive amounts of emulsion and/or sludge; and result in a need for excessive heat to break the emulsion, a need for excessive settling time to resolve the emulsion, reduced capacity of the treating equipment, excessive water remaining in the crude oil causing accumulation of unsalable oil and the resultant cost of retreating the crude, or more difficulty in removing oil from the produced water.

The flow of emulsions at moderate Reynolds numbers through long pipelines has been shown to cause coalescence and develop droplets that exceed 1,000 µm in diameter. The length of the pipeline required to obtain coalescence can be dramatically decreased by using a defined flow path as in the special flow coalescing device shown in Fig. 19.18. The demulsification process may be assisted by the use of baffle plates placed inside the treating vessel. Properly designed and located baffle plates can evenly distribute emulsion in a vessel and cause gentle agitation that may bring about collisions of dispersed water particles to aid in coalescing the droplets. Excessive baffling should be avoided because it can cause excessive turbulence, which may result in increased emulsification and impede waterdroplet settling. Special baffling in the form of perforated plates properly placed inside treating vessels affords surfaces upon which water droplets in the emulsion may coalesce. As the emulsion flows through the perforations, slight agitation in the form of eddy currents is created, causing coalescence. If the perforations are too small, however, shearing of the water droplets can occur, resulting in a tighter emulsion.

Agitation Agitation or turbulence is necessary to form a crude oil emulsion. When turbulence is controlled, however, it can assist in resolving the emulsion. Agitation causes increased collisions of dispersed particles of water and increases the probability that they will coalesce and settle from the emulsion. Caution should be exercised to prevent excessive agitation that will result in further emulsification instead of resolving the emulsion. If the turbulence is kept to moderate Reynolds numbers of 50,000 to 100,000, good coalescing conditions usually should be achieved.

CRUDE OIL EMULSIONS

Other designs of baffle plates provide coalescing surfaces for the water droplets, as shown in Fig. 19.19. Flow through the plates is laminar, but directional changes enable the water droplets to contact the plates and coalesce. Such a device may plug easily and become inoperable quickly. Electrostatic Coalescing The small water drops dispersed in the crude oil can be coalesced by subjecting the water-in-oil emulsion to a high-voltage electrical field. When a nonconductive liquid (oil) containing a dispersed conductive liquid (water) is subjected to an electrostatic field, the conductive particles or droplets are caused to combine by one of three physical phenomena. 1. The water droplets become polarized and tend to align themselves with the lines of electric force. In so doing, the positive and negative poles of the droplets are brought adjacent to each other. Electrical attraction brings the droplets together and causes them to coalesce. 2. The water droplets are attracted to an electrode because of an induced electric charge. In an AC field, be‘cause of inertia, small droplets vibrate a greater distance than larger droplets, promoting coalescence. In a DC field, the droplets tend to collect on the electrodes, forming larger and larger droplets until eventually they settle by gravity. 3. The electric field tends to distort and thus to weaken the film of emulsifier surrounding the water droplets. Water droplets dispersed in oil subjected to a sinusoidal alternating-current field will be elongated along the lines of force as voltage rises during the first half-cycle. As they are relaxed during the low-voltage portion, the surface tension pulls the droplets back toward spherical shape. The same effect is obtained in the next half of the alternating cycle. The weakened film is thus more easily broken when droplets collide. Whatever the actual mechanism, the electrical field causes the droplets to move about rapidly in random directions, which increases the chances of collision with other droplets. When droplets collide with the proper velocity, coalescence occurs. The greater the voltage gradient, the greater the forces causing coalescence. Experimental data show, however, that at some voltage gradient, the water droplet can be pulled apart and a tighter emulsion can result. For this reason, electrostatic treaters normally are equipped with a mechanism for adjusting the voltage gradient in the field. If the quantity of water in the oil is large there is a tendency for the formation of a chain of charged water particles, which may form links between the two electrodes, causing short-circuiting. This is referred to as “chaining” and has been observed in emulsions containing 4% or less water. The short-circuit releases a burst of electrical energy that immediately causes this chain of water particles to become steam. The resulting explosions sound like popping popcorn. If chaining occurs, the voltage gradient is too large (i.e., the electrical grids of the electrostatic treater are too close together or the voltage is too high) for the amount of water being handled. Small amounts of gas breaking out of solution may also create sufficient turbulence and impede the coalescing process. Water-Washing In some emulsion-treating vessels, separation of liquids

Fig. 19.19—Performax TM plate pack, a special coalescing medium for crude oil emulsions.

and vapors takes place in the inlet diverter, flume, or gas boot located at the top of the vessel. The liquid flows by gravity to the bottom of the vessel through a large conductor pipe or conduit. A spreader plate on the lower end of the conduit spreads the emulsion into many small streams or rivulets that move upward through the water, accomplishing a water-wash. After the emulsion has passed through the water-wash, it flows to the upper portion of the vessel, where the coalesced water droplets settle out of the oil by gravity separation. If an emulsion is flowed through an excess of the internal phase of the emulsion, the droplets of the internal phase will tend to coalesce with the excess of the internal phase and thus be removed from the continuous phase. This is the principle on which a water-wash operates. The water-wash is more beneficial if the emulsion has been destabilized by addition of a demulsifier and if the water is heated. The effectiveness of a water-wash greatly depends on the ability of the spreader plate or distributor to divide the emulsion into small streams or rivulets and to cause the emulsion to be in maximum intimate contact with the water bath so that the small drops of water can coalesce with the water. If an-emulsion-treating system or unit uses a waterwash, it can be charged with water to facilitate initial operation. Water from the emulsion to be treated should be used if available. If it is not available, extraneous water may be used.

PETROLEUM ENGINEERING

19-14

Filtering A filtering material with the proper size of pore spaces and the proper ratio of pore spaces to total area can be used to filter out the dispersed water droplets of a crude oil emulsion by preferentially wetting the filtering material with oil and keeping it submerged in oil. When used in this manner, the pack is correctly called a “filter” because it filters out the liquid that it prevents from passing through. When excelsior is used as a filter in an emulsion treater, it is immersed in oil above the oil/water interface level, Excelsior is preferentially wetted by water because of the high affinity the cellulose fibers have for water. If the excelsior is initially wetted by oil, however. the dispersed water droplets in the oil will not normally take possession of the excelsior fibers because the fibers are saturated with oil. If the water droplets do take possession of the excelsior fibers, possession will occur at a slow rate and penetration of the pack by the water will be only partially complete. Excelsior is wood that is cut into small shreds or fibers. Observed under a microscope, the surfaces of each strand of excelsior bristle with tiny sharp barbs. When emulsion flows through an excelsior pack, these rough surfaces cause distortion of the film surrounding the water droplets, thereby encouraging adherence of the droplets to the strands of excelsior. This results in coalescence of the water droplets into drops large enough to settle out of the oil. Excelsior should be made from pitch-free woods. such as aspen, cottonwood, or poplar. Pine excelsior is not recommended for crude oil emulsion-treating purposes. Excelsior should be used at less than 180°F treating temperature. Higher temperature will delignify and deteriorate the excelsior. It will also make it difficult to remove from the vessel. Glass wool and other porous materials have been used as filtering material. Glass wool. when the fibers are properly sized and compacted, can serve as a filtering material for filtering water droplets out of a crude oil emulsion. If the glass wool is coated with silicone, its filtering effect will be enhanced because the silicone-coated fibers will be more wettable by oil than untreated glass wool fibers. Glass wool is not widely used for filtering because of its initial expense and its fouling problems. Porous materials, both plastics and metals, are available that will filter dispersed water droplets from a crude oil emulsion. These porous materials are not widely used because of the difficulty of obtaining and maintaining the proper size pores and because they easily foul and become inoperable. Treating crude oil emulsions by filtering is not widely used because of the difficulty in obtaining and maintaining the desired filtering effect and because the filtering material is easily plugged by foreign material.

Fibrous

Packing

Fibrous coalescing packs are not commonly used in oil treating. They are mentioned for completeness and to differentiate between filtering and coalescence. A coalescing pack is a section or compartment in an emulsiontreating tank or vessel that is packed with a material that is wetted by the water, causing the water to coalesce into larger drops. Separation of two emulsified liquids by use

HANDBOOK

of a coalescing pack operates on the principle that two immiscible liquids with different surface tensions cannot simultaneously take possession of a given surface. The coalescing pack is wetted with or submerged in water. When the dispersed droplets of water come in contact with the water-wet coalescing material. the water droplets coalesce and adhere to the coalescing surfaces. Oil will pass through the pore spaces of the coalescing material. Separation of the two liquids in a coalescing pack is not caused by filtering but by the greater affinity of the waterwet coalescing material for the water droplets. The film of oil containing the emulsifying agent surrounding the dispersed water particles must be broken before these droplets will adhere to a coalescing medium. The film is broken with the aid of demulsifying chemicals and/or heat and by repeated contact between the water particles and the surface of the coalescing materials as the emulsion flows through the pack. When this film has been broken, the water particles adhere to the surface of the coalescing material until they combine into drops large enough to settle out of the oil. Glass wool can be used as coalescing material in emulsion-treating vessels. It will not deteriorate like wood excelsior and will prolong the service life of the coalescing pack. Glass wool fouls rather easily and may cause channeling. Woven wire mesh can also be used but tends to be more expensive than glass wool.

Gravity

Settling

Gravity settling is the oldest, simplest, and most widely used method of treating crude oil emulsions. The difference in density of the oil and water causes the water to settle through and out of the oil. Because the water droplets are heavier than the volume of oil they displace, they have a downward gravitational force exerted on them. This force is resisted by a drag force caused by their downward movement through the oil. When the two forces are equal, a constant velocity is reached that can be computed from Stokes’ law as

)>=

I .78 x 10 -6(A~CIM.)d2 )

... ....

..

(3)

PL, where v=

downward velocity of the water droplet relative to the oil, ft/sec, d= diameter of the water droplet, pm. AY o,,‘ = difference in specific gravity between the oil and water, and CL, - dynamic viscosity of the oil, cp. Several conclusions can be drawn from this equation. 1. The larger the size of a water droplet, the greater its downward velocity-i.e., the bigger the droplet size, the less time it takes for the droplet to settle to the bottom of the vessel, and thus the easier it is to treat the oil. 2. The greater the difference in density between the water droplet and the oil, the greater the downward velocity-i.e., the lighter the oil, the easier it is to treat the oil. If the oil gravity were lO”AP1 and the water fresh, the settling velocity would be zero because there is no gravity difference.

19-15

CRUDE OIL EMULSIONS

3. The higher the temperature, the lower the viscosity of the oil, and thus the greater the downward velocity of the water droplets-i .e., it is easier to treat the oil at high temperatures than at low temperatures (assuming a small effect on gravity difference because of increased temperature). Gravity settling alone can be used to treat only loose, unstable emulsions. When other treating methods destabilize the emulsion and create coalescence, which increases water droplet size, however, gravity settling provides separation of water from oil.

Retention

Time

In a gravity settler, such as an oil-treating tank or the coalescing section of an oil-treating vessel, coalescence will occur. Because of the small forces at work, however, the rate of contact between water droplets is small and coalescence seldom occurs immediately when two droplets collide. Thus the process of coalescence, although it will occur with time, follows a steep exponential curve where successive doubling of retention time results in small incremental increases in droplet size. The addition of retention time alone, after some small amount necessary for initial coalescence. may not significantly affect the size of the water droplet that must be separated by gravity to meet the desired oil quality. A taller tank will increase the retention time but will not decrease the upward velocity of the oil or may not significantly increase the size of the water drop that must be separated from the oil. Thus the additional retention time gained by the taller tank may not materially affect the water content of the outlet oil. A larger-diameter tank will increase the retention time. More important, it will slow the upward velocity of the oil and thus allow smaller droplets of water to settle out by gravity. In this case, it may not have been the increase in retention time that improved the oil quality but rather the reduction in flow velocity, which decreased the size of the water droplets that can be separated from the oil by gravity.

Centrifugation Because of the difference in density between oil and water. centrifugal force can be used to break an emulsion and separate it into oil and water. Small centrifuges are used to determine the BS&W content of crude oil emulsion samples. A few centrifuges have been installed in the oil field to process emulsions. They have not been widely used for treating emulsions, however, because of high initial cost, high operating cost. low capacity, and a tendency to foul.

Distillation Distillation can be used to remove water from crude oil emulsions. The water, along with lighter oil fractions, can be distilled by heating and then separated by appropriate means. The lighter oil fractions are usually returned to the crude oil. The only current use of distillation is in the “flash system” used in 15”API and lower oil. These systems use the excess heat in the oil received from the treater or treating system and convert this sensible heat to latent heat at or near atmospheric pressure. The flashed steam is condensed in a surface condenser in the incoming cooler

stream of raw crude. thus scavenging the excess heat that would ordinarily be wasted. Fig. 19.20 shows a typical flash distillation system for dehydrating emulsions of heavy viscous crude oils. The disadvantage of distillation is that it is expensive and that all the dissolved and suspended solids contained in the water are left in the oil when the water is removed by evaporation.

Emulsion-Treating

Equipment and Systems

The design of equipment or a system for treating crude oil emulsions and the sizing of each piece of equipment for a specific application requires experience and engineering judgment. It would be ideal if a procedure existed that would permit the engineer to infer from measured properties of the emulsion the most economical treating process, taking into account treating temperature, chemical usage, and physical size of treating equipment. Unfortunately, such a procedure is not available and the engineer must rely on experience and empirical data from other wells or fields in the area and on laboratory experiments. For example, the economic balance between the amount of chemical and heat to use to destabilize the emulsion and aid in coalescence is difficult to predict. Almost all emulsion-treating systems use demulsifying chemicals. In most instances, the lower the treating temperature, the greater the amount of chemical required to treat the emulsion. In many areas of west Texas and the Gulf of Mexico, some operators do not add heat to treat the relatively light crudes that are produced. Other operators under the same conditions add heat when treating similar crudes to minimize chemical cost and the size of the emulsiontreating equipment. Another example is the economic balance that must be considered between those factors that promote coalescence (chemicals, water wash, heat, coalescing plates, etc.) and the size of the treating vessels. The larger the size of the treating vessel, the smaller the size of water droplets that can be separated from the emulsion. Thus the use of coalescing aids may reduce the size of the equipment by increasing the size of the water droplet that must be separated from the oil to meet the required quality. The savings in vessel costs must be balanced against the increased capital and operating cost (e.g., fuel and increased maintenance because of plugging) of the coalescing aids. Bottle tests in the laboratory provide a means for estimating ranges of treating temperature and retention time for design purposes. Unfortunately, these tests are static in nature and do not model closely the dynamic effects of water droplet dispersion and coalescence that occur in the actual equipment because of flow through control valves, pipes, inlet diverters, baffles, and water-wash sections. Bottle tests, however, can be useful in estimating treating parameters such as temperature, demulsifier volume, settling time, etc. When evaluating empirical data from similar wells or fields, the designer should recognize that the temperature at which an emulsion is treated may not be as critical as the viscosity of the crude at that temperature. The design of an oil-treating system can be assisted by observing an existing system, knowing the viscosity of the crude at treating temperature, and calculating from the flow gem ometry and Stokes’ law the minimum size water droplet

PETROLEUM ENGINEERING

19-16

150 to 18OOF Production Inlet 15 to 30% cut

HANDBOOK

TEMPERATURE OF SHELL SIDE APPROXIMATELY 20°F

TREATER AT 280°F

r

;c 1

‘FLASH TOWER

CONDENSATE

I 1 1

j-+

WATER

220°F STORAGE

+ Ll Fig. 19.20-Typical

-I

TREATED CRUDE AT 2% CUT

flash distillation system for dehydrating

that can be settled from the crude. A treating system can then be designed that will heat the emulsion to the temperature required to obtain the same viscosity that exists in the sample field, and then any one of the pieces of equipment or combinations thereof described in the next section can be selected and sized so that all water droplets larger than the calculated minimum diameter can be separated from the oil. Because of the uncertainties in attempting to scale up from laboratory data or to infer designs from empirical data from similar wells or fields, a new treating system should be designed with either larger equipment or more heat input capacity than the engineer calculates to be necessary. The amount of “overdesign” to be built into the treating system depends on an assessment of the cost of the extra capacity balanced against the risk of not being able to treat the design throughput.

Description of Equipment Used in Treating Crude Oil Emulsions The characteristics of the emulsion to be treated should be understood before a treating system is selected. Several different types of equipment or systems may satisfactorily resolve an emulsion, but one particular type of equipment or system may be superior to others because of basic considerations in design, operation, initial cost, maintenance

emulsions of heavy viscous crude oils

cost, operating cost, and performance. Effort should be made to select the minimum number of pieces of equipment or the simplest design for each treating system to optimize initial and operating costs. The combination of the various emulsion-treating methods that will provide the lowest use of chemical, lowest treating temperature, lowest loss of light hydrocarbons, lowest overall treating cost, and the best performance should be used. Experience and empirical data may guide the buyer to the optimum combination of treating methods, but field testing will be required to confirm the selection. The following discussion describes various emulsiontreating equipment and systems. Each piece of treating equipment and each treating system affords a wide selection of the type, configuration, size, component selection, component design, and usage. Additional treating equipment can usually be added to each unit or system until the desired treating results are obtained. The design and selection of all the components of the treating system should be made at the time of initial purchase and installation. Because of the modular design of most systems, however, if the selected equipment does not perform as desired or if operating conditions change, additional features can usually be added or operating procedures altered to obtain the desired results.

19-17

CRUDE OIL EMULSIONS

WE13 NIPPLE TO MAINTAIN GAS “CUSHION” IR VESSEL

Fig. 19.21-Typical

Free Water Knockouts Where large quantities of water are produced, it usually is desirable to separate the free water before attempting to treat the emulsion. When oil and water are agitated with moderate intensity and then allowed to settle for a period of time, three distinct phases normally will form: a layer of essentially clean oil at the top with a small amount of water dispersed in the oil in very small droplets, relatively clean water (free water) at the bottom with a small amount of dispersed oil in very small droplets, and an emulsion phase in between. With time, the amount of emulsion will approach zero as coalescence occurs. The free water is the water that separates in 3 to 10 minutes. It may contain small droplets of dispersed oil that may require treament before disposal. Equipment to do this is discussed in Chap. 15. Free-water knockouts (FWKO’s) are designed as either horizontal or vertical pressure vessels. Fig. 19.21 is a schematic of a vertical FWKO. and Fig. 19.22 shows a horizontal FWKO. The fluid enters the vessel and flows against an inlet diverter. This sudden change in momentum causes an initial separation of liquid and gas, which will prevent the gas from disturbing the settling section of the vessel. In some designs, the separating section contains a downcomer that directs the liquid flow below the oil/water interface to aid in water-washing the emulsion.

vertical FWKO

The liquid-collecting section of the vessel provides sufficient time for the oil and emulsion to form a layer of oil at the top, while the free water settles to the bottom. When there is appreciable gas in the inlet stream, a three-phase separator can be used as an FWKO. See Chap. 12 for a description of both vertical and horizontal three-phase separators. Sometimes a cone-bottom vertical three-phase separator is used. This design is used if sand production is anticipated to be a major problem. The cone is normally at an angle to the horizontal of between 45 and 60”. If a cone is used. it can be the bottom head of the vessel, or for structural reasons, it can be installed internally in the vessel. In such a case. a gas-equalizing line must be installed to ensure that the vapor behind the cone is always in pressure equilibrium with the interior of the vessel. Water jets can be used to dislodge and flush the sand from the vessel. Oil and water are usually separated more quickly and completely in an FWKO when the liquid travels through the vessel in a horizontal rather than a vertical direction. Horizontal flow permits a less restricted downward movement of the water droplets. If the emulsion flows vertically upward, the water must move downward through an upward-moving stream; therefore, the downward movement of water is retarded by upward movement of the oil and emulsion.

PETROLEUM ENGINEERING

19-18

HANDBOOK

L.L.C. ;VITHWEIGHTED FLOAT TO SIP II:L?ILAND EMJLSION AND FLOAT ONLY I:;FREE VJATZR.

OIL AND GAS

'wEIf? NIPPLE TO MAINTAIN GAS "CUSHION" IN VESSF3.a PERFORATED WAVE

I~PINGENENT

FLUID IMLST

BREAKER

OUTLET Fig. 19.22-Typical

It is possible to add a heating tube to an FWKO, as shown in Fig. 19.23, or to add heat upstream of the FWKO. In such cases, even though the vessel may be called an FWKO, it is performing the function of an emulsion treater. Many configurations are possible for providing baffles and maintaining levels in an FWKO. A good design will provide the functions described previously, i.e., degassing, water-washing, and providing sufficient retention time and correct flow pattern so that free water will be removed from the emulsion. When the free water is removed, it may or may not be necessary to treat the oil further. In many fields producing light oil, a well-designed FWKO with ample settling time and with a reasonable chemical-treating program can provide pipeline-quality oil. Most often, however, further emulsion treating is required downstream of the FWKO.

Storage Tanks Oil generally should be water-free before it is flowed into lease storage tanks. If there is only a small percentage of water in the oil and/or if the water and oil are loosely emulsified, however, it may be practical to allow the water to settle to the bottom of the oil storage tank and to draw off the water before oil shipment. This practice is not generally recommended or followed. but for small volumes of free or loosely emulsified water on small leases or for low-volume marginal wells, it may be a practical and economical procedure. When a storage tank is used for dehydration, the oil is flowed into the tank and allowed to settle. When the tank is full of liquid, flow into the tank is stopped or

horizontal FWKO.

switched to another tank and the tank is allowed to remain idle while water settles out of the oil. After the water has been separated from the oil by settling, water is drained from the bottom of the tank and the oil is gauged, sampled, and pumped or drained to a truck or pipeline. No water-wash is used in conjunction with the standard storage tank. If there is a water-wash, its shallowness and the absence of a proper spreader causes it to be of little or no benefit.

Settling Tanks Various names are given to settling tanks used to treat oil. Some of the most common are gunbarrels, wash tanks, and dehydration tanks. The design of these tanks differs in detail from field to field and company to company. All contain all or most of the basic elements shown in Fig. 19.24. The emulsion enters a gas separation chamber or gas boot where a momentum change causes separation of gas. Gas boots can be as simple as the piece of pipe shown in Fig. 19.24, or they can contain more elaborate nozzles, packing, or baffles to help separate the gas. If there is much gas in the well stream, it is usually preferable to use a two- or three-phase separator upstream of the settling tank. In this case, the gas boot must separate only the gas that is liberated as the pressure decreases during flow from the separator to the settling tank. A downcomer directs the emulsion below the oil/water interface to the water-wash section. On most large tanks, a spreader is used to distribute the flow over the entire cross section of the tank. This minimizes short-circuiting. The more the upward-flowing emulsion spreads out and

19-19

CRUDE OIL EMULSIONS

BAFFLE

,

BAFFLE

(SOLID?

BAFFLE (SIDE

PERFORATED~ LEVEL

Fig. 19.23--Schematic

CONTROLLER

view of FWKO with heating element in each end

approaches plug (or uniform) flow, the slower its average upward velocity and the smaller the water droplets that will settle out of the emulsion. There are many types of spreader designs. Spreaders can be made by cutting slots in plate, use of angle iron, or holes in pipe. By causing the emulsion stream to separate into many small streams, the spreader causes a more intimate contact with the water to help promote coalescence in the water-wash section. This is shown in Figs. 19.25 and 19.26. Most spreaders contain small holes or slots to divide the oil and emulsion into small streams. Large holes (3 to 4 in. in diameter) will not be nearly as effective in dividing the stream as small holes (‘/8to 1 in. in diameter). In designing a spreader, however, it is important that the fluid is not agitated to the point where shearing of the water droplets in the emulsion takes place, causing the emulsion to become harder to separate. In addition, small holes can be more easily plugged with solids and are difficult to clean. Free-flow coalescing devices, such as S.P. Packs TM (Fig. 19.18), can be installed on the downcomer/spreader to promote coalescence and to minimize shearing of the water droplets by the spreader. As the emulsion rises above the oil/water interface, water droplets settle from the oil countercurrent to the flow of the oil by gravity. Because there may be very little coalescence above the oil/water interface, increasing the height of the oil-settling section above some minimum to aid in spreading out the flow may not materially affect the oil outlet quality.

GAS OUTLET GAS

SEPARATING

G&S

ECUALIZING

WELL PRODuCTtON

ADJUSTABLE IN:fPRPF”CE

OIL SETTLING

Fig.

19.24-Typical settling tank with internal downcomer and emulsion spreader.

1Q-20

PETROLEUM ENGINEERING

rOtL

NOTE -THE

VELOCITY OF WELL FLUID THRU HOLES IN THE DISTRIBUTOR INTO THE WATER WASH SHOULD EXCEED I 0 FT PER SECOND (!I

SETTLING

HANDBOOK

SECTION

NOT

Fig. 19.25-Proper design of well fluid inlet distributor for wash or gunbarrel tank showing use of small holes in dlstributor.

Sometimes oil collectors similar in design to oil spreaders are used to aid in establishing plug flow. The oil collector must not allow vortexing and should collect oil from the top of the tank in such a way that horizontal movement of the oil will be minimized. Some tanks discharge the water through a water collector designed to cause the flow of water to approach plug flow conditions more nearly. The water outlet collector must prevent vortexing of the water and must minimize horizontal movement of the water. The water outlet collector should be located near the tank bottom. There must be enough vertical distance between it and the inlet spreader to allow sufficient clarification of the water, and it should be at least 6 to 12 in. above the tank bottom to allow for accumulation of sand. Some tanks have elaborate sand-jetting and drain systems that may or may not be part of the water-collector system. It may be difficult to make these drains operate satisfactorily because the water flow to each drain must be on the order of 3 ft/sec to suspend the sand. Sand drains may lengthen the amount of time between tank cleanings, but the additional cost of sand drains in tanks may not be warranted. In Fig. 19.24, the oil/water interface is established by an external adjustable weir sometimes called a water leg. The height of the interface is determined by the difference in height of the oil outlet and weir and the fluid properties. It may be calculated from

Fig. 19.26~Improper design of well fluid inlet for wash or gunbarrel tank.

where hM.d = height of water-draw-off overflow nipple in weir box above tank bottom, ft, h 01, = height of clean oil outlet above tank bottom, ft, h M'W= desired height of water-wash in tank above tank bottom, ft, = specific gravity of oil, and Yo Y II = specific gravity of water. Water legs are used successfully for emulsions where the gravity is above 20”API and there is sufficient difference in gravity between the oil and water. Marginal performance is obtained on oil between 15 and 20”API. Below lS”API, water legs normally are not used. It is also common to control the oil/water interface with internal weirs or with an interface liquid-level controller and a water-dump valve. In heavy oils, electronic probes are most often used to sense the interface and operate a water-dump valve. In lighter oils, floats that sink in the oil and float in the water are more common. Not all settling tanks contain all the sections and design details described previously. The choice depends on the overall process selected for the facility, emulsion properties, flow rates, and desired effluent qualities. While Fig. 19.24 is representative of the majority of settling tanks currently in use, other tanks have a different flow pattern. A series of parallel vertical baffles from the bottom of the vertical tank to above the oil level, as shown in Fig. 19.27, cause the flow of the emulsion to be

CRUDE OIL EMULSIONS

horizontal rather than vertical. With this type of flow path, the water droplets fall at right angles to the oil flow, rather than countercurrent to the oil flow. Some settling tank designs employ a vortex or swirling motion at the inlet of the tank to aid in coalescence and settling and to minimize short-circuiting. Many settling tanks employ heat to aid in the treatment process. Heat can be added to the liquid by an indirect heater, a direct heater, or any type of heat exchanger. A direct fired heater, sometimes referred to as a “jug*’ heater, is one in which the fluid to be heated comes in direct contact with the immersion-type heating tube or element of the heater. Direct fired heaters are generally used to heat low-pressure noncorrosive liquids. These units normally are constructed so that the heating tube can be removed for cleaning, repair, or replacement. An indirect fired heater is one in which the fluid passes through pipe coils or tubes immersed in a bath of water, oil, salt, or other heat-transfer medium that, in turn, is heated by an immersion-type heating tube similar to the one used in the direct fired heater. The contents of the bath of an indirect fired heater are caused to circulate by thermosiphonic currents. The immersion-type heating tube heats the bath, which heats the fluid flowing through coils immersed in the bath. When water is used as the bath, water free of impurities will prolong the life of the heater and prevent fouling of the surface of the heating tube and coils. Indirect fired heaters are less likely to catch on fire than direct fired heaters and generally are used to heat corrosive or high-pressure fluids. They usually are constructed so that the heating tube and pipe coil are individually removable for cleaning and replacement. They tend to be more expensive than direct fired heaters. Heat exchangers normally are used where waste heat is recovered from an engine, turbine, or other process stream or where fired heaters are prohibited. In complex facilities, especially offshore, a central heat-transfer system recovering waste heat and supplying it through heat exchangers to all process heat demands is sometimes more economical and may be the only way to meet established safety regulations. Advantages of heating the entire stream of emulsion before it enters the settling tank are as follows. 1. After the fluid is heated, it flows through piping and into the flume pipe or gas boot of the gunbarrel tank. This moderate agitation of the heated fluid can assist in coalescence of water droplets. 2. The emulsion is heated before it reaches the gunbarrel. which aids in removing gas from the oil in the gas boot. This helps maintain quiescence in the settling portion of the gunbarrel. 3. The heater and gunbarrel can be sized independently, which allows flexibility in sizing the system. 4. Water-wash volume in the gunbarrel can be adjusted over a wide range, providing additional flexibility. 5. Continuous flow of fresh fluids through the heater tends to prevent coking and scaling and helps keep the heating surface clean, which will prolong the heater life. Heat can also be supplied to the system by circulating the water in the water-wash section to a heater and back to the tank. The hot-water-wash section warms the incoming emulsion. A thermosiphon caused by density differences of the hot and the cold water can be used as the

19-21

WATER OUTLET [BELOW)

Fig. 19.27-Plan view of vertical tank with horizontal flow settling pattern.

driving force for the circulation if the heat source is not far from the tank. The water also may be pumped to the heater and circulated back through the flume, as shown in Fig. 19.28. In this system, the settling space in the gunbarrel may be disturbed by gas released from the oil when it comes in contact with the hot water. It has two advantages. First, oil will not be overheated because it never comes in contact with the heating element in the heater but is heated by the water bath in the gunbarrel. This minimizes vapor losses from the oil and tends to maintain maximum oil gravity. It also minimizes coking and scaling. Second, this system is as safe from fire hazards as a system involving a fired vessel can be because only water flows through the heater. There is no oil or gas in the fired vessel. Settling or gunbarrel tanks can also be heated directly with a fire tube, as shown in Fig. 19.29, or with internal heat exchangers, using steam or other heat media. Heat exchangers can be either pipe coils or plate-type heating elements. Plate-type heating elements are usually 18 to 32 in. by about 5 to 8 ft. These usually are preferred over pipe coils because the heat-transfer coefficient is 10 to 20% higher for the plate-type heating elements when immersed in oil than for a corresponding area of pipe. Further, the gentle agitation brought about by the convection flow of the oil up the surface of the plate-type element assists in coalescence. Plate-type heating elements are available with a wide range of pressure ratings. They can be purchased for steam service or hot-water service, but the same unit should not be used for both because the construction of the cells is different for the two types of heating media. Pipe coils are popular because of the local availability of materials. The cost is normally slighter higher than for plate-type exchangers, however, especially in larger installations. When settling tanks are heated directly, they operate in much the same manner as vertical or horizontal emulsion treaters.

PETROLEUM ENGINEERING

19-22

HANDBOOK

GAS

t

WELL FLUID INLET -

-AAA--

a-

WA+ER LEVEL I I I

I I I WATER OUTLET

1 GUN BARREL AUXILIARY WELL INLET Fig. 19.29-Heater

P

and gunbarrel in forced circulation method of heating.

Vertical Emulsion

AS OUTLET ,--

DEGASSER

BOOT

e-INLET

I GAS VAPOR

OIL OUTLET

: WATER

Fig. 19.29-Heated

gunbarrel emulsion treater.

OUTLET

Treaters

The most commonly used one-well lease emulsion treater is the vertical unit. A typical design is shown in Fig. 19.30. Flow enters near the top of the treater into a gas separation section. This section must have adequate dimensions to separate the gas from the liquid. If the treater is located downstream of a separator, this section can be very small. The gas separation section should have an inlet diverter and a mist extractor. The liquid flows through a downcomer to the bottom portion of the treater, which serves as an FWKO and water-wash section. If the treater is located downstream of an FWKO, the bottom section can be very small. If the total wellstream is to be treated, this section should be sized for suffkient retention time to allow the free water to settle out. This will minimize the amount of fuel gas needed to heat the liquid rising through the heating section. The oil and emulsion flows upward around the tire tubes to a coalescing section, where sufficient retention time is provided to allow the small water droplets to coalesce and to settle to the water section. Treated oil flows out the oil outlet. Any gas flashed from the oil because of heating flows through the equalizing line to the gas space above. The oil level is maintained by pneumatic or leveroperated dump valves. The oil/water interface level is controlled by an interface controller or an adjustable external water leg. It is necessary to prevent steam from being formed on the fire tubes. This can be done by employing the “40” rule”-i.e., the operating pressure is kept equal to the

19-23

CRUDE OIL EMULSIONS

pressure of saturated steam at a temperature equal to the operating temperature plus 40°F. This is desirable because the normal full-load temperature difference between the fire tube wall and the surrounding oil is approximately 30°F in most treaters. Allowing 10°F for safety, the 40” rule will prevent flashing of steam on the wall of the heating tube. Baffles and spreader plates may be placed in the coalescing section of the treater above the fire tubes. Many treaters were originally equipped with excelsior or “hay” packs. In most applications these may not be needed, but a manway may be provided in case one may need to be added in the field. Although Fig. 19.30 shows a treater with a fire tube, it is also possible to use an internal heat exchanger to provide the required heat or to heat the emulsion before it enters the treater. For safety reasons, some offshore operators prefer a heat-transfer fluid and a pipe or plate heat exchanger inside the treater rather than a fire tube.

Horizontal

Emulsion

Treaters

For most multiwell leases, horizontal treaters normally are preferred. Fig. 19.31 shows a typical design of a horizontal treater. Flow enters the front section of the treater where gas is flashed. The liquid flows downward to near the oil/water interface where the liquid is waterwashed and the free water is separated. Oil and emulsion rises past the fire tubes and flows into an oil surge chamber The oil/water interface in the inlet section of the vessel is controlled by an interface-level controller, which operates a dump valve for the free water. The oil and emulsion flows through a spreader into the back or coalescing section of the vessel, which is fluidpacked. The spreader distributes the flow evenly throughout the length of this section. Treated oil is collected at the top through a collection device used to maintain uniform vertical flow of the oil. Coalescing water droplets fall countercurrent to the rising oil. The oil/water interface level is maintained by a level controller and dump valve for this section of the vessel. A level control in the oil surge chamber operates a dump valve on the oil outlet line regulating the flow of oil out the top of the vessel and maintaining a liquid-packed condition in the coalescing section. Gas pressure on the oil in the surge section allows the coalescing section to be liquid-packed. The inlet section must be sized to handle separation of the free water and heating of the oil. The coalescing section must be sized to provide adequate retention time for coalescence to take place and to allow the coalescing water droplets to settle downward countercurrent to the upward flow of the oil. Fig. 19.32 shows another design of a horizontal emulsion treater with a different flow pattern that minimizes vertical flow of the emulsion. Oil, water, and gas enter the top of the treater at the left side (facing the burners) and travel toward the front and downward. Gas remains at the top, and oil and water are heated as required. Some heat is applied to the water in this section, but because this section has its own temperature controller, it can be regulated up or down for optimum performance. The cross section in Fig. 19.32 shows that the emulsion flows under a longitudinal baffle and through a large slot in the partition plate near the front of the treater at

Fig. 19.30-Schematic

view of typical vertical emulsion treater.

the bottom of the fire tube where it is water-washed. In the right compartment of Section AA, the oil and emulsion flow longitudinally up across the fire tube at about a 10 to 1.5” incline from horizontal. The heating and settling section separation baffle blocks the passage of foam at the top and blocks emulsion at the bottom. Heated oil travels through a slot in a partition that is about at the centerline of the top fire tube. Free water is allowed to travel under the baffle. As emulsion accumulates at the interface, it rises to touch the tire tube, which is only 6 in. above the interface. The fire tube then tends to heat and eliminate the emulsion pad to maintain a uniform emulsion-pad thickness. Channeling, skimming, and stratifying are all reduced by the application of louvered baffles, which are made of a stainless steel sheet punched with a louvered pattern that ranges from 15 to 60% open area. The baffles are solid at the top to prevent foaming or skimming and extend down near but do not touch the water. All the emulsion goes through the louvered openings, which provide a slight impedance to flow to develop even flow distribution and aid in coalescence. Oil level in the treater is maintained by a weir and an oil box. Water level in the treater is critical; thus a weir is placed approximately 5 ft from the rear head seam, and the oil/water interface level upstream of this weir is maintained by the weir. Adjustment of the water-level controller, which is located downstream of this weir, has no effect on the water level in the main treater body upstream of the weir. Because the emulsion flow path in this design is essentially horizontal, the water particles are not opposed by the velocity of upflowing oil as in a treater with a vertical flow pattern. This is especially important in heavy crudes where the differential specific gravity between oil and water is small and the settling velocity is low.

PETROLEUM ENGINEERING

19-24

HANDBOOK

GAS EQUALIZER

MIST

EMULSION INLET

EXTRACTOR

GAS

\

OUT

\” f, _-

,-a-OIL

-------

--------

COLLECTOR

~-----_r’ WATER

+

----

I

WATER

-

SPREADER

WATER OUT

DEFLECTOR AROUND FIRETUBE

FRONT

--I

I

FREE WATER OUT

FIRETUBE

1

OUT ----

COALESCING

SECTION

SECTION

ocLH%

Fig. 19.31-Typical

horizontal emulsion treater with vertical flow

GAS DEMISTER AND COALESCER

FIRE TUBE

OIL WEIR 30 DIFFUSION BAF

/ OIL CONTROLLER

OIL OUTLET WATER OUTLET BURNER EATING AND SETTLING SECTION SEPARATION BAFFLE ELEVATION HEATING CHAMBER 1 y-

DAM

CONTROLLER

HEATING CHAMBER 2 FOR OIL PASSAGE SETTLING SECTION

CENTER BAFFLE -

Fig. 19.32-Horizontal

VESSEL

emulsion treater with horizontal flow.

19-25

CRUDE OIL EMULSIONS

GAS EQUALIZER

MIST

EMULSION INLET

EXTRACTOR

\

\I

GAS

OUT ,--OIL

OUT

---------__ c

COLLECTOR

Di e------

WATER

t

--

-,-

-

WATER -

-

--I

i

I

FIRETUBE

SPREADER FREE

WATER OUT

‘WATER OUT

DEFLECTOR AROUND FIRETUBE Leff .-----

Fig. 19.33-Typical

horizontal electrostatic emulsion treater with vertical flow

Other flow patterns are available if different baffle designs are used in horizontal treaters. The two described previously are examples to show the concepts that are most generally applied. Other methods of heating the emulsion can be used if it is desirable to eliminate the fire tubes.

Electrostatic

Coalescing

1

Treaters

Electrostatic treating can be used in either vertical or horizontal emulsion treaters by including electrical grids in the settling or coalescing sections. Figs. 19.33 and 19.34 show how grids can be installed in the horizontal treaters shown in Figs. 19.31 and 19.32. Two grids of electrodes typically are installed in electrostatic emulsion treaters. One is wired to a source of electric current and the other is grounded. The emulsion flows between these electrodes, which are charged with a very high voltage. The electrodes are installed in the vessel to provide a final stage of coalescence to the emulsion after it has already been treated to near pipeline quality. In the design of Fig. 19.33, the upflowing oil passes the “hot” electric grid, which is usually steel or stainless steel rods or bars spaced 4 to 6 in. apart. This grid is stationary and hangs from multiple electric insulators. AC current is wired to this grid from an external singlephase transformer. The “cold” electric grid is mounted directly above the hot grid and is adjustable from 2.5 to 12 in. from the hot grid. The normal operating spacing between the two grids is usually 4 to 6 in. Coalescing takes place between the oil/water interface and the hot grid, as well as between and above the grids. The oil continues vertically to the outlet collector pipe with

small calibrated holes in the top of the pipe to ensure uniform distribution. The electric section has no oil/gas interface. All gas must be removed in the heating section. The electric coalescing function in the treater shown in Fig. 19.34 is similar to the horizontal grid unit of Fig. 19.33 except that the vertical grids provide the advantage of the horizontal flow pattern for the emulsion and improve the performance of this unit. In addition to the safety controls normally found on emulsion treaters with fireboxes, there are also low-liquidlevel safety switches on the electric treater to avoid the possibility of the electric power being applied when the high-voltage grid is surrounded with gas instead of liquid. The greater the voltage gradient, the greater the forces causing coalescence. Experimental data show, however, that at some voltage gradient the water droplets can be pulled apart and a tighter emulsion can result. For this reason, electrostatic treaters are normally equipped with a mechanism for adjusting the voltage gradient in the field so that the optimum can be obtained. The voltage gradient can be changed (1) by selecting optional transformer voltage taps. (2) by adjusting the voltage gradient by raising or lowering the oil/water inter face in units using horizontal grids-the water level is. in effect, a grounded electrode against which most of the coalescing takes place; or (3) by adjusting the hot or cold grid location to change the voltage gradient. The transformer is normally an 18.000- to 20,000-V secondary, single-phase, oil-tilled. 100%reactance-type transformer. It is mounted on the top, side, or end of the treater with a short, high-voltage conduit connected to an

PETROLEUM ENGINEERING

19-26

Fig. 19.34-Typical

HANDBOOK

horizontal electrostatic emulsion treater with vertical electric grids for horizontal flow of fluids

appropriate entrance probe assembly. The high-voltage line is entirely submerged in transformer oil, which is normally a highly refined hydrocarbon that has been vacuum dried and contains no moisture. The application of electrostatic treaters should be limited to “polishing” of oil to avoid chaining and short-circuiting of the grids. They are particularly effective in reducing the water content of oil to very low levels (less than 0.5 to 1 .O%). Electrostatic coalescence may also aid in reducing heat and/or chemicals required to treat crude oil to a specific quality.

Desalting Crude Oil Most produced water contains salts, which may cause problems in production and refining processes when the solids precipitate to form scale on heaters, plug exchangers, etc. This can cause accelerated corrosion in piping and equipment. In almost all cases, the salt content of crude oil consists of salt dissolved in small droplets of water that are dispersed in the crude. In some instances, the produced oil can contain crystalline salt, which forms because of changes in pressure and temperature as the fluid flows up the wellbore and through the production equipment. Crystalline salt will flow out with the water and is not of importance in desalting operations. The salinity of produced brine varies widely, but most produced water falls in the range of 15,000 to 130,000 ppm of equivalent NaCl. Crude oil containing only 1.O% water with a 15,000 ppm salt content will have 55 lbm salt/l ,000 bbl of water-free crude. The chemical composition of these salts varies, but the major portion is nearly always NaCl with lesser amounts of calcium and

magnesium chloride. Because of the operational problems associated with salts, most refineries buy crude at a salt content of 10 to 20 lbm/l,OOO bbl, then desalt the oil to 1 to 5 lbm/l,OOO bbl before charging to crude stills. The purpose of a desalting system is to reduce the salt content of the treated oil to acceptable levels. In cases where the salinity of the produced brine is not too great, salt content can be reduced by merely ensuring a low fraction of water in the oil. In this case, the terms desalting and emulsion treating are identical, and the concepts and equipment described previously can be used. The required maximum concentration of water in oil to meet a known salt specification can be derived from c,, =0.35c,,y,“f&.,

.

.... ...

..

. . (5)

where C,, = salt content of the oil, lbm/l,OOO bbl, of salt in produced water, c SM’= concentration Pw Y w = specific fW = volume

gravity of produced water, and fraction of water in crude oil.

If the produced brine has a high salt concentration, it may not be possible to treat the oil to a low enough water content (less than 0.2 to 0.25% is difficult to guarantee). In such a case, desalting implies the mixing of low-saltcontent water with the emulsion before treating, as shown in Fig. 19.35. This lowers the effective value of C,, in Eq. 5. If a single-stage desalting system will require too much dilution water, then a two-stage system, such as that shown in Fig. 19.36, is used.

19-27

CRUDE OIL EMULSIONS

MIXER OIL STREAM

Fig. 19.35-Single-stagedesalting

Although it is possible to desalt with most of the emulsion-treating equipment discussed previously, most desalting systems use electrostatic treaters to obtain the lowest possible water content in the oil and thus minimize the amount of dilution water needed. One of the most important parts of desalting systems is the method and efficiency of the method of mixing the wash water with the crude. The smaller the diameter of the wash-water drops dispersed in the oil, the greater the possibility of their coming in contact and coalescing with entrained saltwater droplets. Excessive agitation when mixing the wash water with the crude oil can result in emulsions that are too tight (stable) to resolve easily. Therefore, the amount of mixing provided should be adjustable to zero. This requirement tends to make pumps and level-control valves poor choices for mixing. The most commonly used mixing system consists of some type of special mixing tee or static mixer followed by a globe-type mixing valve. Mixing efficiency in a desalting system refers to the fraction of wash water that actually mixes with the produced water. The remainder of the water, in effect, bypasses the desalting stage and is disposed of as free water. A mixing efficiency of 70 to 85% can be considered a reasonable range of attainment. Part of the energy for mixing is obtained from the pressure of the wash water, which should enter the mixer at approximately 25 psi above the pressure in the vessel.

with dilution water injection.

Reverse Emulsions Most emulsions are the water-in-oil type; they occur much more frequently than the oil-in-water type. Oil-in-water (reverse) emulsions are most likely to be produced where the WOR is high, the dissolved solids content of the water is low, the water is slightly alkaline, and the oil has a naphthenic base. The oil content of these emulsions may vary from as low as a few ppm to 40%. They may vary in consistency from watery thin to a moderately heavy cream. The produced water from some leases and ballast water from some oil tankers contain sufficient oil to be or have the characteristics of an oil-in-water emulsion Such water is usually treated with chemicals formulated for water treating and with equipment described in Chap. 15. Reverse emulsions may not require much, if any, heat. Because the external phase is water, the viscosity is quite low at ambient temperature. The chemicals used to treat reverse emulsions are usually some type of surface-active compounds that will neutralize the charges on the oil particles and allow them to coalesce during the gentle agitation that should follow introduction and mixing of the chemical with the emulsion. Overtreatment of this type of emulsion with chemical can result in stabilization rather than breaking of the emulsion. Empirical data and experience are required to design equipment and/or systems for resolving reverse emulsions.

MIXER

MIXER 1

-a

CLEAN OIL

WATER TO DISPOSAL

DILUTION WATER

OIL STREAM

)

OIL TREATER

-a

OIL TREATER

WATER

D&AL

7

2

OIL TREATERT

DILiTION

WATER

RECiLE

PUMP

Fig. 19.36-Two-stage

desalting using second-stage

recycle.

CLEAN OIL

19-28

Treating

PETROLEUM ENGINEERING

Emulsions

Produced

From EOR Projects

Standard emulsion-treating procedures, equipment, and systems used during primary and secondary oil production may not be adequate to treat the emulsions encountered in EOR projects. EOR methods of oil productionsuch as in-situ combustion and steam, COz, caustic. polymer, and micellar (surfactantipolymer) floods-may result in the production of emulsions that may not respond to treatment normally used in primary and secondary oil production operations. The treatment of the emulsions from EOR projects is usually handled independent of the primary and secondary emulsions from the same fields. Emulsion-treating procedures, equipment, and systems have been and are continuing to be developed for use in these EOR projects.

Clarification

of Water Produced

with Emulsions

Even though a normal (water-in-oil) emulsion exists in the oil production system, when produced water is separated from crude oil, the water usually contains small quantities of oil. The oil has been divided into small particles and dispersed in the water by agitation and turbulence caused by flow in the formation; into the wellbore; through the bottomhole pump, standing valve, traveling valve, and tubing; reciprocation of sucker rods; flow through the wellhead choke, flowline, manifold, oil and gas separator, and treating system; and by surface transfer pumps. These small particles of oil will be suspended in the water and held there by mechanical. chemical. and electrical forces. The amount of oil contained in the untreated produced water in most systems will vary from an average low of about 5.0 ppm to an average high of about 2,000 ppm. In some water systems, oil contents as high as 20.000 ppm (2.0%) have been observed. The oil particles in the untreated produced water will usually vary in size from 1 to about 1,000 pm, with most of the oil particles ranging between 5 and 50 pm in diameter. Nine methods can be used to remove oil from the produced water: chemical, heat, gravity settling (skim tanks, API separators, etc.), coalescence (plate, pipe/free flow), tilted plate (corrugated) interceptors, flotation. flocculation. filtering, and combinations of the above. Refer to Chap. 15 for a discussion of the details of deoiling the produced water.

Operational Considerations for Emulsion-Treating Equipment Burners

and Fire Tubes

The design of burners and fire tubes is of importance because of the high cost of fuel and the operating problems that can occur when they malfunction. The burner should be designed to provide a flame that does not impinge on the walls of the fire tube, but that is almost as long as and concentric with the fire tube. If the flame touches the fire-tube wall. hot spots can develop, which can lead to premature failure. Burners should not be allowed to cycle off and on frcquently because thermal stresses caused by temperature reversals can damage the firebox. The combustion con-

HANDBOOK

trols should be accessible and designed so that the operator can easily adjust the air and gas to achieve optimum tlame pattern and peak combustion efficiency. A reliable pilot burner is required. Many operators and some regulatory agencies require burner safety shutdown valves that will shut off fuel to the burner in case of pilot failure. Unless specifically requested by the purchaser, most small emulsion treaters normally will not include this feature. API RP 14C, “Analysis, Design, Installation and Testing of Basic Surface Safety Systems for Offshore Production Platforms,” contains a basic description of recommended safety devices needed for fired- and exhaust-heated units. Consideration should be given to installing these devices on onshore, as well as offshore, fired treaters. They include process high-temperature shutdown. burner exhaust high-temperature shutdown, lowflow devices and check valves for heat exchangers, highand low-pressure shutdown sensors, pressure-relief valves, flame arresters, fan motor starter interlocks on forced draft burners, etc. Every gas-fired crude oil heating unit should be provided with fuel gas from which liquids have been “scrubbed.” In large facilities, this can be accomplished with a central fuel-gas scrubber or filter providing fuel gas to all fired units. Many small facilities are equipped with individual fuel-gas scrubber vessels for each fired unit. These fuel-gas scrubbers are typically 8 to 12 in. in diameter and 2 to 4 ft tall, and contain a float-operated shutoff valve. If liquid enters the fuel-gas scrubber. the float will close a valve and stop gas flow to the burners of the heating unit. This will prevent oil from entering the combustion chamber and possibly prevent a fire. Most fire tubes that transfer heat to crude oil or emulsion are sized to transfer 7,500 Btuihr-sq ft. although some manufacturers use heat-transfer rates as high as 10,000 Btuihr-sq ft. Fire tubes that transfer heat to the waterwash section of a treater, as in a vertical treater. are sized for 10,000 Btuihr-sq ft, although some manufacturers use heat-transfer rates as high as 15,000 Btu/hr-sq ft. These higher rates are not recommended because they can be overly optimistic and thus may undersize the required fire tube area. The temperature controller. fuel control valve, pilot burner, main burner, combustion safety controls. and fuelgas scrubber for controlling and cleaning the fuel gas for fired treating vessels should be inspected and cleaned periodically as required. A schedule of preventive maintenance is recommended for this equipment. Deposits of soot, carbon, sulfur, and other solids, if any, should be removed from the combustion space periodically to prevent reduction in heating capacity and loss of combustion efficiency. On oil-fired units, the following items should be inspected and maintained periodically: combustion controls, burner nozzles, combustion refractory, air/fuel control linkages. oil pump, oil preheater, pressure and temperature gauges, and 02 and/or CO2 analyzers.

Cleaning

Vessels

Crude oil emulsions may contain mud, silt, sand, salts, asphalt. paraffin, and other impurities produced in conjunction with crude oil and accompanying water. In most

CRUDE OIL EMULSIONS

instances, these impurities are present in small quantities and add little to the treating problem. However, the treating problem may be made difficult and expensive because of the presence of one or more of these impurities in appreciable quantity. Special equipment and techniques may be required to handle these materials. It is good practice to equip all treating vessels with cleanout openings and/or washout connections so that the vessels can be drained and cleaned periodically. Larger vessels should be equipped with manways to facilitate cleaning them. Steam cleaning may be required periodically. Acidizing may be required to remove calcium carbonate or similar deposits that cannot be removed by hot water or by steam cleaning. One of the most likely causes of difficulty in operating fired emulsion-treating vessels is the deposition of solids on heating tubes and nearby surfaces. It is desirable to prevent such deposits, but if they cannot be prevented, these surfaces should be cleaned periodically. The deposits insulate the heating tube, reducing heating capacity and efficiency. Also, these materials may cause accelerated corrosion. Of the salts commonly found in oilfield waters, the chlorides, sulfates, and bicarbonates of sodium, calcium, and magnesium are predominant. The most prevalent of the chlorides is NaCl. Calcium and magnesium chloride are next in quantity. These salts can be found in practically all water associated with crude oil. Salts are seldom found in the crude oil, but if they are present, they are mechanically suspended and not dissolved in it. Emulsion-heating equipment is particularly susceptible to scaling and coking. These processes of deposition are not distinctly separate but may occur simultaneously. Also, one may hasten the other. Calcium and magnesium carbonates and calcium and strontium sulfates are readily precipitated on heating surfaces in emulsion-treating equipment by decomposition of their bicarbonates and the resultant reduced solubility in the water carrying them. These materials will be deposited in pipes, tubes, fittings, and the inside surface of treating vessels. Maximum deposition will occur at the hottest surfaces, such as on heating coils and fire tubes. Scale deposition also may occur when pressure on the fluid is reduced. This is the result of release of CO* from the bicarbonates in salt water to form insoluble salts that tend to adhere to surfaces of equipment containing the fluid. Coke is not generally a primary fouling material. When deposits of salt, scale or any other fouling material build up, however, coking begins as soon as the insulating effect of the fouling material causes the skin temperature of the heating surface (heating tube or element) to reach 600 to 650°F. At this temperature, coke begins to form, which further aggravates fouling and reduces heat transfer. Once coking starts, a burnout of the lirebox may follow quickly. In areas where fluids cause considerable scaling or coking, the amount of such deposits can be reduced to a minimum by decreasing the treating temperature or by use of chemical inhibitors, properly designed spreader plates, and favorable fluid velocities through the equipment. Arranging the internals of the equipment so that all surfaces are as smooth and continuous as possible will also reduce such deposits. The operator should periodically inspect the equipment internally and clean the surfaces as required

19-29

if trouble-free operation is to be obtained over a long period of time. It is impossible to eliminate the deposition of solids entirely in emulsion-treating equipment, but it can be minimized.

Removing

Sand and Other Settled Solids

Sand and silt may be produced with many crude oils. They may settle out in the vessel and be difficult to remove. It is common to shut down and drain the vessel periodically for cleaning. Sand can be removed from the unit with rakes and shovels or with a vacuum truck. The use of “sand pans,” automated water jets, and drain systems can eliminate or minimize the problem of sand and silt in emulsion-treating vessels, but it is very difficult to eliminate sand buildup in large-diameter tanks. Sand pan is the name given to a special perforated or slotted box or enclosure located in the bottom portion of a vessel or tank. Sand pans are designed to cover the area of the vessel that the flow of discharging water will clean. Often they are designed to work in conjunction with a set of water jets. The sand pans for horizontal vessels usually consist of elongated, inverted V-shaped troughs that are located parallel with and on the bottom of the vessels and that straddle the vertical centerline of the vessel. In the design in Fig. 19.37, the sand pans have sides that make an angle of 60” with the horizontal. The bottom edges of the sloping sides are serrated with 2-in. V-shaped slots and are welded to the interior of the shell of the treater. Most sand pans used in horizontal vessels are 5 ft long; a 60-ft-long horizontal vessel will typically have 11 sand pans and 11 sand-dump valves. Sand pans, without a water jet system, have satisfactorily removed sand from most horizontal vessels up to 6 or 8 ft in diameter. Horizontal vessels larger than 4 ft in diameter should be equipped with a water jet system in addition to sand pans to keep sand cleaned from the vessel. Typical sand pans with a water jet system are illustrated in Fig. 19.37. In vertical vessels, the sand pan may be a flanged and dished head approximately one-third the diameter of the vessel in which it is concentrically located. The sand pan is usually serrated around the periphery where it is welded to the bottom head of the vertical vessel concentric with the water outlet. Water jets usually are designed to flow approximately 3.0 galimin of water through each jet with a differential pressure of 30 psi. Standard jets are available for this service that have a 60” flat fan jet pattern. The jets are usually spaced on 12- or 16-in. centers. The water jet header is U-shaped so that the vessel is cleaned on both sides of the sand pan simultaneously. The water jets can be programmed for all the jets to flow at the same time, or they can be controlled by operation of the water jets and the sand dump valves in sequential cycles. One problem in removing sand from vessels is that very few, if any, water-discharge control valves can withstand the abuse of sand-cutting during the water-discharge period for the long term. The partial answer to this problem is to arrange the instrumentation to open and close the water-discharge control valve on clean sand-free water and to use special slurry-type valves. The most sophisticated sand-removal systems use programmable logic controllers. This solves the problem of selection of the proper time intervals between dumps

PETROLEUM ENGINEERING

19-30

Fig. 19.37-Sand

pans and water jet system in a horizontal vessel.

and automatically controls the length of the water/sand discharge. The timing must be coordinated with the water jet system and the normal water-dump controller. A properly designed sand-removal system with proper water jetting and water/sand dumping can operate for many years without the need for a shutdown to clean out the sand or to repair or replace the dump valve. Most emulsion-treating systems that handle large volumes of sand should not rely on hand or nonprogrammed operation for removal of the sand. If the operator fails to activate the dump valve often enough, the sand will cover the sand pans and plug or partially plug the water outlet, and the drains will become inoperative. With sand pans in the treater but without a programmer, large volumes of sand will usually cause trouble by plugging or partially plugging the water outlets and/or by cutting or wearing the drain valve. Because both the amount and type of sand vary greatly, the length and frequency of the water-jetting and dumping cycles must vary to suit local conditions. Most of the coarser sand will settle out in the inlet end of the treater; the fine sand will settle out near the outlet end of the treater. It may be necessary to cycle the water jets and drain valves near the inlet end of the treater three to four times more frequently than those near the outlet end of the unit. Many timers are set for 30 minutes between jetting and dumping cycles and for 20- to 60-second jetting and dumping periods.

Interfacial

HANDBOOK

buildup may contain paraffin, asphaltenes, bitumen, water, sand, silt, salt, carbonates, oxides, sulfides, and other impurities mixed with the emulsion. It can be rem moved from the vessel through a drain installed at the interface. The most common procedure, however, is to close the water dump valve and float it out to a bad-oil tank for further processing or disposal. Interfacial buildup can also be discharged with the water by opening the water-drain valve.

Corrosion Emulsion-treating equipment that handles corrosive fluids should periodically be inspected internally to determine whether remedial work is required. Extreme cases of corrosion may require a reduction in the working pressure of the vessel or repair or replacement of vessel and piping. Periodic ultrasonic tests can measure the wall thickness of vessels and piping to detect the existence and extent of corrosion. Corrosion of emulsion-treating equipment is usually mitigated or controlled by a combination of the following.

Exclusion

of Oxygen. Corrosion rates in most oilfield applications can be kept low if O2 is excluded from the system. Care must be taken in the process design to install and maintain gas blankets on all tanks in the process and to exclude rainwater from the system. Recycled water from sump systems and storage tanks is a prime source for 02 entry into the process.

Buildup

Interfacial buildup, sometimes referred to as sludge, is material that may collect at or near the oil/water interface of emulsion-treating tanks and vessels. Interfacial

Corrosion

Inhibitors. An inhibitor is a material that, when added in small amounts to an environment potentially corrosive to a metal or alloy, effectively reduces

CRUDE

19-31

OIL EMULSIONS

the corrosion rate by diminishing the tendency of the metal or alloy to react with the solution. Inhibitors, in the form of liquid solutions or compounds, can be injected into the flow stream in the flowline, manifold. or production systern to inhibit corrosion that would occur otherwise.

Cathodic Protection. Sacrificial galvanic anodes are commonly used for cathodic protection. They are made of a metal that will provide sacrificial protection to the steel vessel because of its relative position in the galvanic series. Most galvanic anodes used in emulsion treaters are about 3 to 6 in. in diameter and about 3 to 4 ft long. Multiple anodes usually are installed in each vessel. The anodes usually are sized to last from 10 to 20 years. They are considered expendable and are always installed in the vessel through a flange or quick coupling so that they can be easily replaced when expended. The galvanic anodes must be installed so that they are immersed in the water, which serves as an electrolyte. They will not protect the treater if they are immersed in the oil. The anodes must “see” all metal surfaces that are to be protected-i.e., there must be no obstructions between the anodes and the surface they are to protect. Each anode should be located as near the center of the compartment or area they are to protect as practical. An impressed electric-current cathodic protection systern can also be used to inhibit corrosion. It is a direct electric current supplied by a device using a power source external to the electrode system. The DC current can be obtained by rectifying AC current. When resistivity ol the electrolyte ranges from 25 to 300 Q.crn and above. consideration should be given to the use of an impressed current system. Impressed current systems are difficult and costly to maintain. however. and usually require skilled technicians. Electrical current density requirements for cathodic protection of emulsion-treating vessels usually range from 5 to 40 mA/sq ft of bare water-immersed steel.

Internal Coating. Emulsion-treating

vessels can be coated internally for protection from corrosion. It is important that the internal surfaces and the welds of the vessels be properly prepared to receive the coating. A coating system must be selected that will withstand the physical and chemical environment to which it will be exposed. Coating specifications. application techniques. and final inspcction are very important considerations. Most coating systems will contain some holidays (breaks in the coating) or may be damaged in shipping or installation. Therefore. coating alone should not be relied on to prevent corrosion. Steel tanks can be galvanized or lined in the field with fiberglass or other coatings. Some operators use fiberglass tanks in their emulsion-treating process, while others feel that this represents an unnecessary fire hazard.

Special Metallurgy. In particularly severe environments, such as where large quantities of CO: are cxpccted and where O1 cannot be practically eliminated from the system. it is possible to minimize corrosion by using stainless steel vessels or an internal stainless cladding in carbon steel vessels. In most low-pressure applications, stainless vessels are less expensive than clad vessels. It may also bc cheaper to use a stainless vessel than one that is internally coated because of the labor required to prepare and to coat the internal surfaces of the vessel.

Level Controllers

and Gauges

A wide selection of liquid-level controllers is available for liquid/gas control and for oil/water interface control in light crude oil (above 20”APl) systems. For interfacial controllers in light crude oils. floats that sink in the oil but float in the Later normally are used. For heavy crude oils, electronic interface controIIers have been very successful. These operate on the principlc of the differences between oil and water electrical conductivity, electrical capacitance, or radio frequency. The most common type is called “capacitance probes”; they USC the dielectric strength of the fluid in which they arc immersed. Standard gauge glasses (reflex or transparent) are used on 20”API crude oil and higher. Reflex gauges normally are used on liquid/g% levels and transparent gauges for oil/water levels. Armored gauge glasses normally are used on pressure vcsscls and tubular gauge glasses on tanks. Some operators use the tubular gauge glasses on low pressure treating equipment. Tubular gauge glasses nor mally are furnished on standard low-pressure vessels unless armored gauges are specified. For API gravities below 20”APl, gauge glasses are not recommended. particularly for interfacial service. because they are difficult or impossible to read. In lieu of gauge glasses. a system of sample valves is used with the sample lines all piped to a single point just above a sample box. Generally, the lines are insulated to keep them warm. A nameplate is clamped on each sample valve to dcsignate the elevation it represents in the treater. The sample box is fitted with a drain line piped to the sump.

Water-in-Oil

Detectors

(BS&W Monitors)

Several companies manufacture devices for detecting and measuring the water content of crude oil. They are commonly called BS&W monitors. BS&W monitors are typically analog instruments that measure dielectric strength and are specifically designed for determination of the water content of crude oil containing a low percent of water. They do not operate satisfactorily on streams containing free water. The unit provides a water reading car responding to the water content of the oil. It can be made to alarm, record. and control if the detected percentage exceeds the field-selectable preset limit of BS&W content.

Special Safety Features

for Electrostatic

Treaters

Because of the high voltage and the associated potential hazard to personnel that can result from entering a drained vessel with the grids activated, electrostatic treaters require a positive shutdown switch for the high-voltage transformer. This disconnects the transformer if the fluid lcvcl falls below a predetermined level in the treating vessel. Some manufacturers install an internal grounding device inside the treater that grounds the hot grid if fluid is not present.

Changing

Excelsior Packs

Excelsior used in treating emulsions may have a serviceable lift ranging from just a few days to several years. The best grade excelsior should be used because cost of the excelsior is small compared to the expense of removing and replacing it. In some fields. the excelsior must be chopped into blocks with an ax and removed in chunks.

19-32

Serviceable life of the excelsior may be extended by periodically washing it with hot water. The water level can be allowed to build up above the top of the excelsior pack and the water heated to about 2 10°F. The temperature should be kept this high for about I hour. The water should be drained quickly from the vessel while it is hot. The hot water may carry most of the foreign material with it. If the application of heat only partially cleans the excelsior, a second heating may clean it further. Care should be taken to use water that will not deposit solids in the treater while it is being heated.

Economics of Treating Crude Oil Emulsions The object of operating oil-producing properties is to deliver consistently the maximum volume of highest-APIgravity oil to the pipeline at the lowest possible cost. Emulsions should be prevented wherever feasible and treated at the lowest cost where they cannot be prevented. Implementation of the following directives can minimize the occurrence of emulsions and the costs of treating. 1. Eliminate production of water with oil where possible and practical. 2. Minimize the investment in emulsion-treating equipment by studying the treating problem and the selection and use of appropriate treating methods, equipment, and procedures. The emulsion treating system should be as small as possible, yet capable of adequately handling treating requirements on the lease. Treating systems may be initially oversized to allow for future development. lease expansion, or increased water production. Such anticipation of future needs should be considered when treating equipment is purchased; however, needlessly oversized systems involve unnecessary expense and accomplish nothing that properly sized systems will not accomplish. 3. Minimize the loss of oil with water and salvage oil from interfacial sludge and tank bottoms where feasible. Oil may be discharged with the water as it flows from FWKO’s, emulsion treaters, gunbarrels, or other treating vessels. The fraction of oil is low and the oil is usually dispersed in small droplets. Sometimes this oil is pumped along with the water to disposal wells or delivered to operators of water disposal companies without recovery or without credit being received by the lease. This oil loss can be minimized by maintaining proper operating variables with adequately sized and maintained vessels and controls and by properly designed water treating systems. 4. Minimize chemical treating costs by use of the most appropriate chemical demulsifier compound(s), the optimum quantity of chemical, the proper location and method of injection of chemical, the proper means of intimately mixing chemical with emulsion, and the proper use of heat. Treating chemicals are not recoverable and constitute a continuing expense. Some crude oil can be adequately treated by chemical injection used in conjunction with coalescing and/or settling without heat. However, some emulsions require an increased temperature during the coalescing and settling period. A proper balance of chemical and heat aids in providing the most economical and efficient treating system. The chemicals must be intimately mixed with emulsion so that a minimum amount of chemical will provide maximum benefit. Chemicals may be wasted by being injected into the oil in large slugs and not intimately mixed with the emulsions.

PETROLEUM ENGINEERING

HANDBOOK

5. Ensure that chemicals added to the produced fluids are compatible. Some corrosion inhibitors can cause emulsions or affect the action of oil-treating chemicals. Chemicals used in produced-water-treating systems may be recycled to the oil-treating system with the skimmed oil and cause emulsion-treating problems. 6. Conserve gravity and volume of oil by using optimum treating temperature, cooling oil before discharging to storage, discharging vent gases from treating vessels through cooler oil in stock tanks. maintaining slight gas pressure on treating system and storage tanks, and using vapor recovery equipment on vessels and tanks. Crude oil emulsions should be resolved at the lowest effective temperature. Excessive heat drives condensible vapors from the oil, and they are discharged with the gas. Loss of these light ends lowers the API gravity of the oil and simultaneously reduces the oil volume. A further disadvantage of overheating is the increased maintenance rcquired on treating systems caused by hot spots. salt deposition, scaling, and increased rate of corrosion, especially of the fireboxes. 7. Use all treating equipment to the best advantage. By careful observations, supervision, and record keeping, emulsion-treating equipment can be used to maximum efficiency, Transfer of equipment and alterations or additions to the treating system may be made to use existing equipment better. Constant testing and vigilance are required to obtain maximum results. 8. Practice preventive maintenance to minimize irretrievable loss of oil production because of downtime for equipment repairs. The more complex the treating system, the greater will be the possibility of mechanical failure. Oversized and overly complex systems have a greater failure frequency than more appropriately designed, simpler, and more compact systems. 9. Exchange information on treating methods and results among company personnel, with other operators, engineering firms, vendors, and chemical-treating companies. Experience can be gained and shared by personnel responsible for handling treating problems, which will result in lower treating costs. Cost records are important in oil emulsion-treating operations. To achieve optimum operation of emulsiontreating equipment at minimum cost, proper records must be kept of operating temperatures, pressures, fuel and/or power consumption, chemical usage, performance, etc. Such records should be kept on a daily, weekly, or monthly basis, reviewed regularly, and kept available for supervisory personnel. Cost records make it possible to predict whether an existing system should be modified or replaced. Justification for modifying or replacing an existing system will depend on the efficiency of the system, and this can be determined best from accurate and reliable cost and performance records. Cost records on existing methods or systems will assist in determining the type, kind, and size of treating systems for new leases. Treating cost records should make it possible to determine current operating costs, probable installation costs for new systems, and probable future operating costs of similar systems. Each operator should determine what is to be charged to emulsion-treating costs. Listed in Table 19.2 is an outline of items that may be considered part of the data base for a cost-accounting system. Some of these items will

19-33

CRUDE OIL EMULSIONS

not be applicable to all treating systems, and some operators may elect to group some of the categories. A comprehensive general listing is presented for those who wish to consider all items of cost. Special systems and conditions may require additional cost items. It is necessary to consider all factors listed in Table 19.2 if complete and accurate treating cost records are to be compiled. This information should be obtained and recorded on a continuous daily, weekly, or monthly basis, and it must be accurate and concise if cost records are to be of maximum value. Investment costs must include the initial cost of all equipment used, including the cost of transporting it to the location, of erecting and installing the equipment, and of readying the system for operation. Such items as pipe and pipe fittings, valves, grade work, foundations, and fencing should be included. The labor cost should include supervisory personnel, cost of company gang and contract gang, and other labor required to obtain, install, and put the treating system into operation. Operating cost should be kept separate from maintenance cost and should include such items as supervisory labor, operating labor, chemicals, fuel, and miscellaneous supplies. Maintenance cost should include cost of maintaining and repairing all treating equipment. This should include such items as cleaning. repairing, painting, and other similar items. The Overall System Performance section should include an accurate record of the volume of oil treated and the volume of water separated, treated, and handled. This part of the record should also include reference to troubles experienced with the system and a commentary on day-today performance of the unit or system.

Key Equations in Metric Units Q=53.09aT(0.5y,,y,,+y,,.y,,.),

.

.

(2)

where Q is in watts. ilT is in Kelvin. y,, is in m’ld. y,, is dimensionless, (I,,. is in m j/d. and yII. is dimensionless.

,‘Z

5.43x

Equipment Investment Costs Material Treating equipment and facilities Auxiliary equipment, controls, and accessories Labor to install equipment

Company labor Contract labor Other expenses Surface rights Special services Other Operatmg Costs Material Chemicals Chemical injection equipment Diluents and solvents Testing apparatus Depreciation allowances Other Labor Supervisory Operator or pumper Steaming or cleaning crew Gang Contract Other Other expenses Equipment rental Fuel (gas or liquid) Electric current Transportation Laboratory expenses Other Maintenance Costs Material Maintenance Replacements and additions Repalrs Labor Supervisory Pumper or operator Mechanic Painting Gang Contract Other

Overall System Performance

10 -‘o(Ay(,\,)d2 .

(3)

where 1’ is in m/s. AY l,il is dimensionless. d is in pm. and p,, is in Pa.s.

P.L. and Bcshlcr. D.U.:

OF EMULSION TREATING

Other Expenses Equipment rental Transportation Other

CL il

Bmdxd..

TABLE 19.2-COSTS

“Cold Trealing of Oilfield

Einul-

\ionr,” presented;~tthe SouthwehlernPetroleun~ Short Courw. Dcpr. ot Purroleu~n Englncerinf. Tcx;r\ Tech U.. Luhboch. April 1975

Volume of oil treated Water content of treated oil Volume of water produced Volume of water treated Volume of oil salvaged from water treatment Remarks or observations

19-34

PETROLEUM

Bechcr. P : Priwiples of’ Emulsion Twh~toio~y, Corp.. New York City (1955).

Reinhold Pubhhhing

ENGINEERING

HANDBOOK

McCiaflin, G. el ul.: “The Replacement of Hydrocarbon Diluent With Surfactant and Water for the ProductIon of Heavy, Viscous Crude Oil,” JPT (Oct. 1982) 2258-64.

Besaler. D.U.’ “Demulsification of Enhanced Oil Recovery Produced Fluids,” Tretolite Div.-Petrolite Corp., St. Louis, MO (March 23. 1983).

McGhee. E.: “Una Sola Planta Deshidratara 150,000 BPD,” Interameritnno (Aug. 1965) 42-46.

Blair. C.M.. “Handling the Emulsion Problem in the 011 Fields.” Magna Corp.. Santa Fe Sprmgs, CA (Dec. 6, 1971).

Mennon, V.B. and Wassan, D.T.: “Demulsifications,” Encyclopedia ofEwl.sion Technology, P. Becher (ed.), Marcel Dekker, New York City (1984) 2.

Blair, C.M.: “lnterfdclal Films Affecting the Stability of Petroleum Emulsions,” Chemi.w,v and Indu.stryv(1960) 538-44.

Breuking Emdsions by Chemical Technology-Thuorws Erwkin#, Technology Sugarland. TX (1983).

Series

CTS-V3,

Nalco

of Emu/;rmn

Chemical

Co.,

Coppel. C.P.: “Factors Causing Emulsion Upsets in Surface Facllitles Following Acid Stimulation,” JPT (Sept. 1975) 1060-66.

Corrmion. L.L. Shreir (ed.), John Wiley and “Corrosion Control.” Sons Inc.. New York City (1963) 2, 18.12. Cwwsion Cwzrwl iu Prrroleum F’n~~wtion. NACE TPC5. Natl. Assn. of Corrosion Engineers, Houston (1979).

Item 5 I 103.

Corrtnio/~ Inhrhirors. Item 5 1073. Natl. Assn. of Corrosion Engineers, Houston (1973). CO, Corrosion in Oil und Gas Production: S&wed Pup~rs, Abstrcrcts, and Refprewes. Item 51 120. Natl. Asan. of Corrosion Engineers. Houston (1984). “Demulsification.” (1975).

Tretolite

Div.-Petrollte

Corp..

St. Louis.

MO

“Design, Installation. Operation. and Maintenance of Internal Cathodic Protection Systems in Oil Treating Vessels,” NACE Standard RP-05-75, Natl. Assn. ofcorrosion Engineers, Houston (Oct. 1975). Fontaine, E.T.: “Oilfield Handling Equipment.” 41-44.

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H, S Cormsiorz in Oil und Gas Production: A Cmpilarion of Ciasr~c Puperr, Item 51113, Natl. Assn. of Corrnslon Engmeers. Houston (1981).

hwoduciion IO Oiljrkl Corrosion

Wufer Twhnology, Item 52 140. Natl. As&n. of Engineers, Houston (1979).

Pew&u

J.L., Collie, B., and Black, W.: Surface Activity, the Physical Chemistry, Technical Applications. and Chemical Constitution of S~ntheti~Surfare-Artive Agents, D. Van Nostrand Co. Inc., Prince-

Moilliet,

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“New Mechanical Coalescing Medium is Used in Treaters,” Gas J. (Jan. 23, 1984) 82-83.

Petrov, A.A. and Shtof, I.K.: “Investigation of Structure of Crude Oil Emulsion Stabilizers by Means of Infrared Spectroscopy,” Chrmical Technology Fuels Oils (July-Aug. 1974) 10, No. 7-8, 654-57. “Practices and Methods of Preventing and Treating Crude Oil Emulsions,” Bull. 417, U.S. Bureau of Mines, Superintendent of Documents. Washington, D.C. (1939). “Recommended Practice for Analysis, Design. Installation. and Testmg of Basic Surface Safety Systems on Offshore Production Platforms,” latest edition, API RP 14C, API. Dallas. “Recommended Practice for Analysis of Oil-Field Waters.” tion, API RP 45, API, Dallas.

latest edi-

“Recommended Practice for Design and Installation of Offshore Production Platform Piping Systems,” latest edition, API RP l4E. API, Dallas. “Specification for Indirect-Type Spec. 12K. API. Dallas.

Oil Field Heaters.”

“Specification for Vertical and Horizontal edition. API Spec. l2L. API. Dallas.

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“Standard for Welding Pipelines and Related Facilities.” API Std. 1104, API, Dallas.

latest

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Stockwell, A.. Graham. D.E.. and Cairns, R.J.: “Crude Oil Emulsion Dehydration Studies,” paper presented at the 1980 Oceanology lntl.. Brighton, England, March 2-7, available from BPS Exhibitions Ltd., London, England.

Twaiing Oil Field Emulsions, third edition, Petroleum Extension Service. U. of Texas, Austin (1974).

Jones. T.J . Neuatadter, E.L.. and Whittingham. K.P.: “Water-in-Crude Oil Emulsion Stability and Emulsion Destabilization by Chemical J. C&z. Per. Twh. (April-June 1979) 17, No. 2, Demulsltiers.” lot-08. Mansurov. R.I. ef rrl.: “Sravnitel’Nye lapytaniya Elektrodegldratorov Trekh Konstruktsll (Comparatwe Tests of Three Differently Deslgned Electrodehydrators).” Nefi Kho: (Dec. 1976) No. 12. 50-53.

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