Method for processing water for extraction of oil by thermal methods. RU patent 2247232.

FIELD: oil extractive industry.

SUBSTANCE: method includes first stages of capturing energy of processed heat from high pressure steam separator, placed below steam generators. Then transfer of heat energy into heated separator and evaporator and heat exchanger is performed for distillation of bed water present in oil-bearing bed and restoration of distillated water and concentrated salt solution or hard product. Concentrated water steam from heated separator is circulated through evaporator and heat exchanger to support from 1% to around 50% of steam mass in the flow, returning into heated separator, and prevent pollution and forming of scale. Equipment includes separator for processed low pressure energy, heated separator and steam compression with forced circulation circuit to produce distillated water.

EFFECT: higher efficiency.

6 cl, 2 ex, 1 tbl, 13 dwg

The present invention relates to a highly efficient method of water distillation and install for this method, and more specifically, the present invention relates to a highly efficient method of distillation of water used for crude oil production by thermal methods, which get minimal clogging and the formation of scale in operating the equipment over a long period of work.

In different regions of the world production of crude oil, hydrocarbon material having a substantially higher viscosity or measured in degrees American petroleum Institute (API) lower density (less than 20° ANI, typically 7-12° ANI)than traditional crude oil, is more time consuming and requires a high thermostimulation underground natural reservoir. More specifically, in Western Canada producers of crude oil used injection into the reservoir of steam under high pressure at a typical pressure of about 1500 to 3000 psi (105,5-210,9 kg/cm 3 ), and in some cases 150 psi (10,55 kg/cm 3 ). thermal energy of steam generated by the plant, known as the steam generator, up to 60-80% quality steam, Inuktitut in a vertical or horizontal system of wells to reduce the viscosity of crude oil. Flowing crude oil collected in the adjacent producing wells and a combination of crude oil, emulsion oil/water, condensed steam and formed by hard water (known as produced water) supply to the surface. Using ground equipment, crude oil is separated from process fluids and derive for commercial sale.

Produced water typically extracted in a ratio of water/oil from 2 to 5, usually dropping into the hole to reset commercial wastewater. Add water from a source of groundwater that is authorized by the resolution, is used to power a steam generator. Typically requires a minimum clearance of added water to reduce the hardness and quantity of compounds of silicon dioxide in order to avoid the formation of scale on the surfaces of the heat exchanger of the steam generator and to prevent the danger of a breakdown. In some systems, equipment concentrated produced water from the drain of the steam generator is separated from the injection into the reservoir of steam and discharged into suitable deep wells for wastewater disposal. Such concentrated produced water is also called tarannum thread. This prevents the injection tank is excessive and unnecessary amounts of hot water during exposure. Typical, presently used methods of extraction of crude oil are way cyclic exposure (CCS or Hull n’ Puff) and the way gravity drainage using a pair (SAGD)..

In connection with public requirements and rules manufacturers of heavy oils must carry out the regeneration and reuse of water, and some companies require zero discharge of wastewater. This means that 100% of the water used shall be recovered and reused and no wastewater is not subject to descent outside of designated development. Produced water extracted in separation of oil and steam separators, high pressure, contains components of hardness, dissolved and suspended silica and colloidal compounds (clay), and dissolved solids such as sodium chloride. If such salt water recycling without treatment, exposed the work of the steam generators due to clogging and fouling.

Another problem facing by using the method of stimulation steam for extraction of crude oil, is the fact that to increase oil recovery with increasing operating temperatures productive collectors from 230 to 400° F (110-204,4° (C) the temperature of the extracted fluid (oil and water) increases. To facilitate the customary practice for atmospheric oil separation and water create a significant amount of water vapor when the pressure of the fluid decreases. This water vapor is typically condense by external means, such as air cooler, for extracting condensed water. thermal energy of condensation of steam is released into the atmosphere as waste.

Until the present invention the combination of energy recovery exhaust heat with a highly effective way of distillation water purification, which do not clog equipment, recycling of produced together with crude oil, water and waste saturated salt solution was technically and commercially limited.

Basically, distillation water treatment is a highly effective way of evaporation of pure water distillate and extraction of the concentrated liquid or solid substances containing a large number of non-volatile components. This method can be an effective means of extracting purified water from contaminated sources. However, the method of distillation water purification usually has several disadvantages, and they are all connected with contamination of equipment or a mass scale because of the presence in the subject distilled fluid minerals or other components. Conventional forming a solid precipitate compounds include calcium, magnesium and silicon. Pollution or to a greater extent, the formation of a solid precipitate on heat transfer surfaces has a deleterious effect on the heat-conducting components, incapacitating the conventional distillation.

In U.S. patent 4566947 from 28.01.1986 disclosed conventional method of distillation, but do not specify the main factors necessary for the prevention of pollution, or the application of the method for purification of produced water, which is the companion component in the extraction of heavy oils. The most important place in this patent is the count of 7, starting at line 55, about 4, which States the following: “the Method which uses steam compressor 307 in this way is advantageous when the feed liquid promotes the deposition of solid substances by condensation of its volatile component or clogging material, such bake that may cause an accident or cause time-consuming repair and maintenance of the compressor. Using the scheme described above equipment only vapor from the evaporator passes through the compressor 307, thereby preventing the occurrence of such problems. The inner part of the pipe 350 and the evaporator 352 can be maintained in a clean condition using suitable means of cleaning. The above method has advantages especially when the residual liquid is water, since it is possible to add through line 353 cheap, not requiring regeneration process water. When the water that collects in the bottom of the column 306, does not contain substances that contaminate the inside of the compressor 307, it can be fed to the evaporator through line 353 to maintain a constant liquid level in the evaporator.

4 of this patent is reproduced below, as well as additional figure (modified Figure 4), essentially corresponding to Figure 4, which includes the device presented by the applicants, for the implementation of this method.

As can be seen from a consideration of Figure 4 of the said patent and devices applicants, superimposed on a schematic of this patent, if the patent U.S. No. 4566947 to add a schema to a forced circulation evaporator and the determination of the specific flow ratio pair, representing the residual liquid water may contain contaminants and work without impurities or prevent scale formation on heated surfaces.

Figure 4 of the said patent piping 340 and 353 are not connected. No connection bottom part 306 with the pipeline 353. Section 306 in the column determine how the bottom part of the column containing residual liquid with a predetermined concentration of ammonia. In this patent it is noted the fact that the method has advantages, especially when residual liquid is water. It is assumed that these figures do not offer and do not determine the nature of the circulation residues from the bottom of the column. There is only a General mention of the threads 34 and 35 in column 3, lines 19 to 23. Indicated that the residual liquid in the column 1 is directed to the evaporator through the pipe 34 and the heated residual liquid through the pipe 35. In addition, in line 20 indicates that the liquid residue from the bottom of the column is heated by receiving heat from condensation of the compressed vapor. After a careful study of the description of this invention has found that it does not contain any mention of the ratio of vapor or vapor and liquid.

In the mentioned patent clearly States that if the water that collects in the bottom of the column does not contain polluting substances, this water can be fed into the evaporator. The present invention does not depend on the nature of the feed stream that is associated with the possibility of clogging of the evaporator. Water contaminated with pollutants, impurities, can be fed directly to the evaporator without fear of its clogging or other damage to the heat exchanger. Actually it is the opposite of what is stated in the patent. When considering loop diagram in figure 4 of the patent, all of the heated surfaces associated with liquids accumulating on the bottom of the tower depicted in the installation never in contact with anything else, besides water, is essentially not containing contaminating the equipment of pollutants, while this water is used as the main medium for removal of ammonia from a mixture of ammonia and water. In the reference patent at column 3, line 19"... the residual liquid of the column 1 is directed to the evaporator 8 through line 34 where it is heated by receiving heat from condensation of the compressed [in this way] the pair of the compressor 7, while the heated residual liquid circulating in the bottom of column 6 through line 35".

If you combine the information in columns 7, above, with the directions of the columns 3, the result will only clogging of the installation. In U.S. patent No. 4566947 by combining these steps, information that can only bring to the clogging of the installation. In contrast, the method presented in this invention effectively provides a system in which take contaminated by impurities incoming stream that contains water and serve it in a setting without any fear of contamination of the surfaces of the heat exchanger.

This is possible in light of the recognition of the nucleate boiling and the importance of this physical phenomenon is to maintain a wet surface in the circuit including the heat exchanger. As you know, the bubble regime boil for accumulations of water at atmospheric pressure is highly specific region, forming a separate bubbles. It was defined in the reference paper Principles of Heat Transfer, Third Edition, Frank Kreith; and Heat Transfer, Seventh Edition, J.P.Holman.

Reference Principles of Heat Transfer on str discusses relatively stable film and nucleate boiling. In this passage refer to Figure 10-2, as illustrating nucleate boiling. It is obvious that the individual bubbles are formed on the wire shown in the figure. This phenomenon is also illustrated in Fig.9-5 str second reference document. Heat Transfer. In this link the author actually acknowledges on p.519 that there is considerable divergence of views on the mechanism of nucleate boiling. In this case recognizes the importance of maintaining the nucleate boiling. This concept is important for maintaining the wet surface heat exchanger, and this contributes to the fact that the ow containing any pollutants that are not in contact with the surface of the heat exchanger and there is no risk of clogging. When the pair share is more than 50%, the heat exchanger is really clogged.

Below technology cleans the incoming stream containing contaminating impurities. Clogging impurities in the incoming flow can come into direct contact with the surface of the heat exchanger without any clogging. This last feature is not possible in the invention to the specified U.S. patent by his own admission. This is an excerpt from the description presented above. It is the recognition of the above principles is what allows this method to achieve the desired results. The method of this patent simply does not apply to this invention.

Another common problem typical methods of distillation water purification is the need of consumption of large amounts of energy. Without an energy source of waste heat and means effective regeneration of this energy consumption, the energy required is equivalent to the latent heat of vaporization of water at a given pressure or temperature. Water distillation under such conditions can not be a commercial method used to improve water quality. Target species when extracting crude oils are high-energy streams of fluid, suitable as sources for energy recovery of waste heat.

To solve the problems associated with traditional methods of distillation, you must consider the following variables. The following three equations represent the basic dependence of the heat transfer within the system water distillation:

On (total) =U· A· LMTD (1)

Q (found warmth) =m· CP· (T1-T2) (2)

Q (latent heat) =m· L (3)

where Q=quantity of heat transmitted (WTG h -1 (TU=British thermal unit))

U=overall heat transfer coefficient or the ability of the system to heat transfer (BTU h -1 ft -2 F -1 )

A=surface area of heat transfer (ft 2 )

LMTD=mean logarithmic value of the temperature differential or heat transfer systems (F)

m=mass flow rate of the liquid in the liquid or gaseous state (lb -1 hour )

CP=specific heat of fluid (BTU h -1 F -1 )

T1, T2=temperature of fluid entering or leaving the system (F)

L=latent heat of evaporation or condensation (BTU lb -1 )

In order to get an efficient distillation system, the number of exchanged and recycled heat Q, expressed by the above equations must be maximized, but at the same time observing practical limitations to other variables and to the prevention of fouling and clogging. For a particular fluid and dynamics of fluid within a heat exchange installation variables U, Cf and L are relatively unaffected. Therefore, to solve the problems associated with distillation purification containing impurities of water, special attention should be paid to the variables A, Q/A, LMTD, m, and T1 and T2.

In order to completely solve the problems associated with distillation containing the impurities of the water of the means of production of crude oil and thermal method, and to prevent the formation of scale, in addition to the basic equation above, it is necessary to consider other factors:

transform efficient energy sources of waste heat;

the rate at which heat is transferred within the distillation system, known as the flow of heat or QA -1 (BTU h -1 ft -2 );

the level of impurities in the concentrate;

the final boiling point of concentrate relative to the saturation temperature vaporizing steam;

the degree of saturation and the level of deposition of the concentrate;

the level of evaporation evaporating steam.

Prior to the present invention an efficient energy recovery of waste heat from the means of production of crude oil and to maximize the number of transmitted and recovered heat for the distillation water purification, in which there is no tendency to clogging or fouling could not be implemented for a long time.

Was developed in a way that is both energy efficient and eliminates the problem of scale formation, which was previously encountered in the distillation water purification, containing, among other such contaminants as organic compounds, inorganic compounds, metals.

The invention further develops the concept identified in the initial application. Still the concept was linked to two different concepts, including distillation or multipurpose distillation water treatment using vapor recompression and recycling of waste heat in combination with a unique heat recovery scheme. It was found that by further consolidation of the recovery of low-grade thermal energy from the installation of crude oil thermal method with having a unique configuration schema regeneration and heat transfer with forced convection can be obtained very favorable results, namely obtaining maximum heat transfer, excluding or minimizing the need for energy compression and maintain the desired schema forced convection so as to prevent conduction, leading to the formation of scale on heat exchangers, which typically occurs in the practical application of conventional methods of distillation.

It was found that the energy use of waste heat from the installation of crude oil can be regenerated in the scheme of heat transfer, and this source of low-grade energy, which in most cases were discharged as excess energy or non-regenerating energy use to reduce or reduce to zero the number of required compression for treatment of waste water and significantly reduce commercial benefits of this method.

According to the presented methodology source of energy descent vehicle what is used is the high pressure fluid from the separator high-pressure steam, which is evaporated to reduce the pressure of obtaining low-grade steam and hot water reservoir at a pressure of 10-15 psi (0,7-1 kg/cm 2 ). Low pressure steam is used in a heated separator as a heat source for evaporation of purified water, which is then condensed to produce high quality water for submission to the steam boiler. Hot concentrated otmerenny stream is used to preheat the incoming stream of produced water before it enters the heated separator.

In addition, from the discharge of pressure fluid coming from the tank for crude oil, receive a significant source of waste energy. The pressure of the working fluid, usually when they exit the tank 50-300 psi (3,5-21,09 kg/cm 2 ), dropping to about atmospheric separator degassing. Working fluids oil/water transfer in normal atmospheric separation of oil/water, known in the art. Waste energy can be extracted in two ways.

If the method of production of crude oil is not used to transport the gas, and after the wellhead in the working fluids present only a minimal amount of associated gas, the exhaust steam is separated from the tank degassing and served in a highly efficient distillation unit for energy recovery of waste heat. If used to transport the gas in the wellbore to obtain crude oil and/or working fluids is a relatively large amount of associated gas, then the energy of the waste heat can be regenerated using suitable means of heat and pass through a hot fluid in a highly efficient distillation unit for energy recovery of waste heat. In this example, the cooled working fluid environment Tegaserod in the tank degassing without appreciable loss of steam. The existing state of the art for methods of thermal stimulation is the growing mode in the reservoir oil to increase production of crude oil, which gives a higher temperature working fluid in the wellbore of the production well. These temperatures reach levels typically above 230-400 mesh° F (110-204,4°) and even 500° F (260° C). Therefore, a significant amount of regenerated energy waste heat is available as a source for installing high-efficiency distillation water purification..

The technical result of the present invention is to provide an improved efficient extraction of produced water for the distillation purification of water containing organic and inorganic compounds, metals and other polluting compounds, resulting in purified water fraction that does not contain impurities, and in addition does not lead to the formation of scale in installation of distillation.

This technical result is achieved in that the method of obtaining energy for treatment of water used in the extraction of crude oil from oil-bearing formation containing crude oil and water, according to the invention, includes the following stages:

a) providing an incoming flow of water;

b) processing the incoming water stream to form a vapor fraction and a liquid fraction;

C) the use of preseparator for separating a vapor fraction and a liquid fraction;

g) separating a vapor fraction and a liquid fraction;

d) the use of a separator of oil and water and install water distillation;

(e) the discharge into the tank vapor fraction;

g) the collection of crude oil and produced water from the oil layer in the separator of oil and water;

C) separation of crude oil and produced water from the separator;

and) supply of thermal energy contained in the fraction of liquid to the distillation of water;

K) treatment of produced water in the installation of water distillation.

The incoming water flow condition prior to its contacting with steam. The incoming water flow condition to remove mineral impurities.

Crude oil from step C) has a density of from 7 to 20° on the scale of the American petroleum Institute.

The method may additionally include the stage of use of the heat exchanger for receiving at least part of thermal energy in the liquid fraction.

The method may further include stage preheat the incoming water flow through at least part of the energy received from the heat exchanger.

Crude oil may include gravity drainage method of extraction using steam.

Crude oil may include a method of cyclic steam stimulation.

Crude oil may include a method of Stripping steam and gas.

The above technical result is also achieved and what is provided is a method of obtaining energy from equipment for extraction of crude oil contained in the oil-bearing formation, while the energy of the water treatment obtained when the extraction of crude oil, with the method according to the invention contains the following stages:

a) use source a pair containing a vapor fraction and a liquid fraction;

b) the use of separator oil-water and install water distillation;

C) injection into the reservoir, at least part of the vapor fraction and the liquid fraction to extract crude oil;

g) collecting crude oil and water from the oil layer in the separator of oil and water;

d) separation of crude oil and produced water from the separator;

(e) filing with the installation of water distillation thermal energy contained in the liquid fraction;

g) treatment of produced water in the installation of water distillation.

The method of obtaining energy in the processing of crude oil for water purification, obtained by extraction of crude oil, according to the invention, includes the following stages:

a) providing a bleed stream of high pressure;

b) instantaneous evaporation purge flow high pressure stream of waste energy low pressure and concentrated otvarennogo stream;

C) evaporation of produced water using flow waste energy low pressure;

d) preheating the stream of produced water using concentrated otvarennogo stream;

d) providing a circuit for circulation of a fluid medium, comprising a heated separator and evaporator heat exchanger, connected by means of the fluid flow;

(e) passing the preheated incoming stream of produced water in a heated separator;

g) passing the waste energy in the evaporator for heat energy;

C) evaporation flow of produced water using waste energy in the evaporator-heat exchanger to form a vapor fraction and a concentrated liquid fraction containing impurities;

and circulation, at least part of the concentrated liquid fraction through the evaporator-heat exchanger and the heated separator to maintain a ratio of the mass of concentrate to vapor fraction from 300 to 2, resulting in a gain from about 1% wt. to less than 50% wt. output fraction vapor from the evaporator-heat exchanger in order to prevent clogging and fouling in the evaporator;

C) condensation of the vapor fraction external condensing means;

l) collecting fractions of the condensed steam and the flow of waste energy, essentially does not contain impurities.

Selectively, you can use the compressor for condensing part of the faction pair up with distilled water when the quantity of waste energy is sufficient for the heated separator.

The method may include the stage of passing the vapor fraction in the crystallizer solids to extract the energy contained in the vapor fraction to form a solid contaminants in the mould of non-volatile compounds present in the concentrated liquid fraction containing the impurities.

The method may include stage bandwidth fraction of steam in the external condenser to condense vapor into liquid.

The number containing impurities wastewater may be equivalent to the amount of waste energy obtained by this method.

The incoming stream may be subjected to the scheme of pre-testing before preheating. The scheme of pre-processing can be selected from the group comprising the following: filtration, ion exchange, gravity separation, chemical treatment and steaming.

The method may optionally include the stage of exposure to the condensed distillate scheme further processing.

The scheme further processing can be selected from the group comprising the following: filtration, ion exchange, advanced oxidation, adsorption and aeration.

The above mass contains about 10% wt. the concentration of steam.

Steam can condense in the heat exchanger plate-plate.

The next aspect of the present invention is a method of obtaining energy in the processing of crude oil for processing water obtained during the extraction of crude oil, according to the invention, contains the following stages:

a) providing a bleed stream of high pressure;

b) instantaneous evaporation purge flow high pressure stream of waste energy low pressure and concentrated otvarennogo stream;

C) evaporating at least part of the produced water using flow waste energy low pressure;

d) preheating of produced water using concentrated otvarennogo stream;

d) providing a schematic flow of a fluid medium, comprising communicating the heated separator and evaporator heat exchanger;

e) ensure that the scheme vapor flow, including the heated separator means of the compressor and the evaporator is a heat exchanger communicating with each other;

g) passing the preheated brine water in a heated separator;

C) evaporating the preheated brine water using waste energy of low pressure and compressed steam vapor in the evaporator heat exchanger to form a vapor fraction and a concentrated liquid fraction;

and) development faction pair formed by using waste energy of low pressure with external tools condensation;

K) removing any remaining fraction of steam by means of the compressor;

l) circulating at least part of the concentrated liquid fraction through the evaporator-heat exchanger and the heated separator to maintain a ratio of the mass of concentrate to vapor fraction from 300 to 2 for output fractions of vapor from the evaporator-heat exchanger in an amount of from about 1% wt. to less than 50% wt. in order to prevent clogging and fouling in the evaporator-heat exchanger;

m) collecting fractions of the condensed steam and the flow of waste energy, does not contain impurities.

And another additional aspect of the present invention is a method of obtaining energy in the processing of crude oil for processing water obtained during the extraction of crude oil, according to the invention, contains the following stages:

a) providing a bleed stream of high pressure;

b) instantaneous evaporation purge flow high pressure stream of waste energy low pressure and concentrated otvarennogo stream;

C) evaporation of produced water using flow waste energy low pressure;

d) preheating of produced water using concentrated otvarennogo stream;

d) providing a circuit for circulation of a fluid medium, comprising a heated separator and evaporator heat exchanger communicating with the fluid flow;

(e) passing the incoming stream of produced water in a heated separator;

g) passing a stream of waste energy low pressure in the evaporator;

C) evaporation of produced water using waste energy of low pressure in the evaporator-heat exchanger for the formation of the first vapor fraction containing the impurities concentrated liquid fraction;

and circulation, at least the part containing the impurities concentrated liquid fraction through the evaporator-heat exchanger and the heated separator to maintain a ratio of the mass of concentrate to vapor fraction from 300 to about 2 with obtaining the output fraction of vapor from the evaporator-heat exchanger from about 1% wt. to less than 50% wt. in order to prevent clogging and fouling in the evaporator;

K) using the crystallization and the evaporator-heat exchanger connected by using the vapor fraction;

l) removing the part containing the impurities concentrated liquid fraction for submission to the means of crystallization;

m) passing the vapor fraction in the evaporator to provide heat energy for the deposition of solids from containing impurities concentrated liquid fraction;

h) formation of the second vapor fraction from crystallization and vapor from the essentially solids;

a) condensing the second vapor fraction by means of the capacitor;

m) collecting the condensed first vapor fraction and a condensed second vapor fraction and a condensed stream waste of energy.

Additional advantages of this technique are zero cost. Get it due to the fact that it becomes possible to use a sufficient number of low-grade waste energy, and therefore, when cleaning produced water, there is no need to use compressor. In addition, this method helps to extract 100% water, the result is zero the amount of waste water containing in solution impurities, as impurities converted into solid waste.

And another aspect of the present invention is a method of obtaining energy for treatment of water used in the extraction of crude oil from oil-bearing formation containing crude oil and water, according to the invention, contains the following stages:

a) providing an incoming flow of water;

b) processing the incoming flow of water for the formation of fractions of water vapor and liquid fraction;

C) provision of preseparator for separating fractions of water vapor and liquid fraction;

g) the division of fractions of water vapor and liquid fraction;

d) the use of a separator of oil and water and install water distillation;

e) forcing the fraction of water vapor in the reservoir;

g) pressure drop in the flow of crude oil, produced water and water vapor coming out of the oil-bearing formation;

h) transfer of energy contained in the water vapour in the installation of water distillation;

and separation of crude oil and formation water.

The method may additionally include the stage of supply of thermal energy contained in the liquid fraction, the installation of water distillation.

And another aspect of the invention is a method

energy to treat the water used in the extraction of crude oil from oil-bearing formation containing crude oil and water, according to the invention, contains the following stages:

a) providing an incoming flow of water;

b) processing the incoming flow of water for the formation of fractions of water vapor and liquid fraction;

C) the use of preseparator for separating fractions of water vapor and liquid fraction;

g) the division of fractions of water vapor and liquid fraction;

d) the use of a separator of oil and water and install water distillation;

e) forcing the fraction of water vapor in the reservoir;

f) obtaining thermal energy of crude oil and produced water coming from the oil reservoir by means of heat exchange;

C) separation of crude oil and formation water;

I) filing with the installation of distillation of thermal energy from the heat exchanger;

K) filing with the installation of water distillation thermal energy contained in the liquid fraction;

l) processing of produced water in the installation of water distillation.

It was found that by precisely controlling the amount of circulating mass to exceed the fraction of vapor leaving the evaporator from less than 300 to about two times, can be realized by some desired benefits:

1. Concentrate circulating through vyparivalsya side of the evaporator will contain precisely controlled amount of steam from about 1% to 50% by weight of the circulating concentrate.

2. When precise control of the quantity of steam to increase the temperature of the circulating concentrate remains very low (about 1° F) and the heat exchange surface of the evaporator remains wet at a temperature close to the temperature of the circulating concentrated liquid. This reduces the risk of contamination of these surfaces.

3. In this controlled low amount of steam concentrated liquid in the heat exchanger is subjected to the action even more reduced localized concentration ratio of less than 1.1, thus avoiding localized deposition forming scale compounds on the surfaces of the heat exchanger.

4. As the education of the mass of vapor in the direction of the outlet of the evaporator speed of vapor passages of the heat exchanger significantly increase, thus contributing to good mixing and, consequently, reducing the risk of clogging.

5. When controlling the amount of vapor in the vaporizing fluid, it is possible to make a significant heat transfer through the latent heat without scale formation and crossing temperature inside the heat exchanger.

6. Because it remains a very small temperature increase vyparivaya side of the evaporator is maintained average logarithmic value of the temperature differential or heat transfer of the evaporator and thereby retained very little need for the incoming energy.

7. By regulating the flow of heat temperature wet surfaces for condensation and vaporization is maintained close to the temperature condition of saturated steam at modes of evaporation and condensation. The type of boiling may be different from the initially forced convection to a stable bubble evaporation wet wet surfaces.

8. By providing funds evaporator for adsorption is carried low grade waste heat energy from the funds of the heavy oil requires less energy to compress, provided that sufficient blowing under high pressure.

In one embodiment of the invention, in its broad scope, distilled water is evaporated and passed through a strainer to remove any drops held, where it is condensed by using external tools. The flow of waste energy enters the evaporator where it condenses to distillate. Thermal energy transfer recirculating the concentrate from the heated separator, where by controlling the ratio of the mass of the circulating concentrate to the steam flow so that it ranged from less than 300 to about 2, formed less than 50% of a couple, or more specifically less than 10% steam in the circulating flow of the concentrate. The steam formed in the circulating concentrate, absorbs heat transmitted through the latent heat of evaporation, at the same time preventing the temperature rise of the circulating concentrate more than 1° F.

Pure distilled water, collected from the external condenser and evaporator-heat exchanger at a temperature and condensation pressure is returned in the high quality of the water supplied to the steam generator. At the same time a portion of the concentrate stream is removed from the heated separator to regulate the desired concentration of non-volatile contaminants. This concentrated stream from which the released steam, at a pressure and temperature of the heated separator is passed through a heating device to transmit the remaining energy of the heat content of the incoming stream of produced water. Additional techniques pre-and post-processing can be applied as a continuous or batch methods for removal or treatment of contaminants before, after, or in the distillation process. You can use the methods of pH control and other chemical additives for ionization of volatile components or changes in the terms of dissolving the concentrate in order to further improve the distillation according to the present invention. You can regenerate a significant amount of distilled water, typically more than 90% of the incoming flow of water. When additionally using tools crystallization reach 100%regeneration. With regard to the breadth of this method, it is easily applicable to any operation of crude oil using steam for thermal stimulation, for example in the traditional method of flooding the ferry, the method of cyclic steam stimulation (CSS or Huff n’ Puff), the way gravity drainage using a pair (SAGD) and push the steam and gas (SAGP).

This list is in any case not exhaustive and is provided only as an example.. Next the invention will be described in more detail with reference to the accompanying drawings, in which:

figure 1 depicts the diagram of a method generally in accordance with one implementation of the present invention;

2 is a diagram of the method as a whole in accordance with another variant of implementation of the present invention;

figure 3 - scheme of installation of water treatment for the method according to the invention;

4 is an alternative embodiment of the method of figure 2;

5 is an alternative embodiment of the installation according to figure 3;

6 is a schematic illustration of typical conditions of pressure and temperature around the components of evaporation;

Fig.7 - curve process of condensation or evaporation system evaporator-heat exchanger;

Fig diagram of the flow for the evaporator-heat exchanger plate/plate type;

Fig.9 is a diagram illustrating the level of evaporation in the evaporator, taking place in the circulating fluid, depending on the ratio of the mass of circulating fluid to the mass of water vapor;

figure 10 is a diagram illustrating the resulting effect was localized concentration in the evaporator when the change in the number pair;

11 is a diagram representing a data test pilot distillation;

Fig diagram of the method as a whole in accordance with the following one implementation of the present invention;

Fig diagram of the method as a whole in accordance with another alternative implementation of the present invention.

In figure 1 will be presented to one embodiment of the present invention. Supplied to the steam generator 125 collect water in the supply tank 110 to the water. Water is taken from a suitable source 105 groundwater, or it may be water 100, which recycle or type of traditional processing methods, such as lime softening and alkaline impurities, softening by ion exchange or distillation. First, from the feedwater must be removed components hardness, such as calcium, magnesium or silicon dioxide to prevent the formation of a solid residue on the steam generator 125 high pressure. An additional consideration is that the dissolved solids should be less than 8000 parts per million (by weight) to obtain high-pressure steam of the desired 80%quality. Total dissolved solids (TDS) consists mainly of sodium chloride. The volumetric amount of water can vary from a low number average of 10,000 barrels per day (BPD) (159· 10 4 liters per day) for pilot plants to extract heavy oil thermal methods to more than 100,000 BPD (159· 10 5 litres per day) for commercial extraction of crude oil by thermal methods.

Air-conditioned water from the reservoir 110 is pumped by means of a number of forcing pumps 115 in the steam generator 125 high pressure. A typical steam generator 125 generates steam quality 60-80% at a pressure from 1000 psi to 3000 psi (70-210 kg/cm 2 ) or more, depending on the nature of the oil-bearing formation. This type of oilfield steam generator known in the art, is limited to less than 100%quality steam due to the specific design and limitations associated with the formation of scale in the pipeline. To generate saturated steam or steam 100% quality or superheated steam can be used other evaporators, traditional steam boilers and evaporators, which simultaneously regenerate the heat if high quality water, such as distilled water, is commercially available.

In some reservoirs of crude oil, for example, the reservoirs of crude oil using the method gravity drainage using a pair cannot be pumped into the formation of pairs is less than 100% quality without the operation of extraction of oil. For these operations, use the separator 130 high-pressure steam to separate the saturated vapor 135 from the liquid phase 140 high pressure, which is also called superheated brine. Some tools use of the energy available at position 140, by heat exchange at position 120 is supplied into the steam generator water before lowering the pressure. The number of recovered thermal energy depends on the level of steam pressure at position 135, but mostly it is limited to a small number.

So in most ways gravity drainage, which is used for the production of crude oil, there is a significant amount of energy is waste heat stream 140, which has limited application, and such heat is typically directed to a cooling tower or cooling apparatus as waste heat. This thread is waste of energy can be brought in the installation of 180 highly efficient water distillation for treatment of produced water 175, which significantly affects the reduction of the commercial value of water treatment and improvement of production costs in the extraction of crude oil. Most important, however, are the environmental benefits are that in this way you can exclude add water and containing impurities of water and a significant part of the waste energy can be regenerated, which reduces power consumption flue gas and total emissions of air.. 135 Pairs of high pressure pump in the reservoir 145 through the barrel 150 wells. Depending on how crude oil production configuration wells may be different. Figure 1 shows a typical way to gravity drainage location where the steam is injected into the horizontal wellbore, and the extracted liquid containing crude oil extracted in the adjacent horizontal shaft 155 wells. Produced fluids take on the surface and transmit operating pipelines 160 in the installation 165 oil recovery. Crude oil, having a density of less than 20° ANI and more 7° ANI, extract and commercially sell for refining.

Produced water 175 received in a typical ratio of water to oil is from 2 to 5, served in the installation of 180 water treatment. Produced water contains sodium chloride, silicon dioxide, dissolved organic hydrocarbons, calcium and magnesium, which primarily arise from a natural oil reservoir and source initially added water.

Containing concentrated salt solution waste water or solid substance that can be extracted from the installation 180 water treatment in the form of a stream 185.

This stream typically has no commercial value and requires a reset on site or outside of the development, depending on the placement of equipment for crude oil production.

Usually the installation of 180 highly efficient water distillation water treatment regenerates from more than 80% to 100% of produced water in the form of pure distilled water in the stream 100.

Figure 2 shows another variant embodiment of the present invention. This option provides the equipment for crude oil production, where the requirements to the temperature of the produced fluid after stem 155 of the production well and the mouth of 160 wells such that the temperature should be higher than normal 230° F (110° (C) up to 400° F-500° F (204-260° (C) in order to increase oil production. Hot extracted from the well fluids pass through the separator 161 degassing at a time, reducing the pressure at position 162, for their submission to the installation of the separation of oil and water. Water vapor is formed from the separator 161 degassing at a typical pressure of 40-60 psi (2.8 to 4.3 kg/cm 2 ) (usually less than 100 psi (7 kg/cm 2 ). This low-grade pairs 163 served in the installation of 180 highly efficient water distillation water treatment for use in the evaporation of distilled water from produced water. The method of obtaining heat can be used if the number of collateral and/or the pressurized carrier gas is low in relation to the water vapour formed from the extracted from the borehole fluid 160.

If, in the main, are not faced with a large enough number of associated gas in crude oil, and/or transporting gas artificially pump in the shaft 155 of the production well, in this case, you must use the reserve method of obtaining energy. Produced hot fluid medium is passed through any suitable means of heat transfer to a sharp reduction in temperature before entering the separator 161 degassing. Energy waste heat extracted from position 164 using a suitable transfer medium and passed through the flow 166 in the installation of 180 highly efficient water distillation water treatment water treatment with obtaining distilled water.

As shown in figure 2, both methods generate heat using threads 140 and 166, can be used separately or in combination depending on the operating conditions of the natural oil layer 145 and the benefits of using each of these methods.

Next, with reference to figure 3 is a variant embodiment of the installation of 180 highly efficient water distillation water treatment.

The ow 175 produced water serves on stage 12 pre-treatment to remove insoluble substances, volatile substances and/or implementation of other steps to regulate the pH or conditioning for pre-processing the incoming stream 175. Volatiles released from the feed stream at position 14, while the less volatile components discharged from the incoming stream at position 16.

Pre-processed incoming stream coming from position 12, then through device 18 pre-heating to raise the temperature of the incoming stream in order to increase heat recovery before the introduction of the heated separator 20. The ow can be divided into several streams and pass through other secondary devices pre-heating and increased heat recovery to maximise the recycling potential of the plant. This scheme will be understood by specialists. Several devices preheating can be configured as a single MSM heating device or separate devices 18 and 26. Single incoming streams are again combined and heated to conditions close to the heated separator, before the flow enters the heated separator 20. If desirable, the ow can also enter into the flow of forced circulation to create in the evaporator of the dilution effect. The heated separator may include multiple device separation, for example a cyclone separator. The lower section 22 produces a cyclonic action for suspension of solid material in the concentrate and feed of what is called tarannum flow or concentrate, as shown by line 24. Consumption otvarennogo stream 24, a continuous or periodic controls the concentration of the components in a heated separator 20, thereby adjusting the degree of saturation of the concentrate, the degree of supersaturation corresponding to the precipitation of solids and boiling temperature in a heated separator 20.

Otmerenny stream 24 at a temperature and concentration specified in a heated separator 20, is passed through the secondary heating device 26 for heat recovery for the incoming stream 28. Otmerenny restore stream to a temperature within about 3° F (-16° (C) to get closer to the incoming stream 12 and produces a stream 185..

The top section of the heated separator 20, containing mainly saturated water vapor, is designed for the separation of vapor and liquid and may contain such distinctive features as the mesh filter layer or turbine unit (not shown) for the coalescence of liquid drops from the steam flow. Steam escaping from the heated separator 20 and generally indicated by the line 30, is ecologically pure distillate and, depending on the components present in the incoming stream may consist of potable water or water that is suitable for use in the evaporator. Part of the steam is transferred to the compressor 32 to raise the temperature and pressure of water vapor to a temperature exceeding the temperature of the heated separator 20. At the outlet of the heated water vapor separator may be under any pressure, including vacuum. The steam is initially saturated in terms of the heated separator 20, however, it can become supersaturated, if the concentrate contains the components in a concentration sufficient to raise the temperature of boiling steam. This concept is known as raising the boiling point and it must be understood so that appropriate compensation compression. The additional energy provided water vapor contributes to the establishment of the necessary average of the logarithmic values of the temperature differential or thermal treatment required for the implementation of heat transfer in the evaporator-heat exchanger 34. Any remaining portion 46 of steam passed to any suitable external device 58 condensation recovery steam in the form of distilled water at position 48.

The compressor or blower 32 can be any device known in the art, which can induce a gas pressure of from about 3 to 15 psi (0,211-1,055 kg/cm 2 ) in the steam flow and the flow of the desired amount of steam. The pressure of the gas, which must be obtained from the compressor 32, specifically determined for each installation taking into account the conditions of evaporation in a heated separator 20 and the required average of the logarithmic values of the temperature differential to the evaporator 34. Steam coming out of the compressor 32, mainly is superheated steam. The degree of overheating depends on the pressure at the output and efficiency of the compressor unit 32. Waste energy in the form of saturated steam, low pressure, typically at a pressure less than 100 psi (7.03 is kg/cm 2 ), more specifically less than 50 psi (3,515 kg/cm 2 ), can be added to the compressed couple before entering the evaporator-heat exchanger 34. The combined stream reduces the degree of overheating posed by the compressor.

The evaporator is a heat exchanger 34 provides a condensation of the combined steam flow received from the compressor 32 and the source 51 waste of energy for distillation sludge from the evaporator 34 in the receiver 36 of the condensate. This is the stage of energy capture heat and latent heat of the combined steam flow and transfer it by means of a heat transfer circulating the concentrate stream 38. The distillate accumulated in the receiver 36 is essentially saturated liquid at a definite temperature and pressure. Additional heat contained in the distillate, recovered by passing the hot distillate using a pump 40 back through the device 18 preheating, where effluent stream is cooled to about 3° F (-16° (C) in the incoming stream from the position 12. Distilled water from the receiver 36 and 48 can be combined to generate a significant heat before entering the device 18 is heated, and it is released in the form of stream 100.

It was found that using a pump 42 for circulating the concentrate, which circulates a set quantity of concentrate from the heated separator 20 through evaporative heat exchanger 34, you can get significant benefits without excessive concentration of the concentrate and without the risk of clogging or fouling on the surfaces of the heat exchanger. The ratio of the mass of the circulating concentrate to a few specifically selected within less than 300 to about 2, to get the exact amount of generated steam from about 1% to less than 50% in the stream 38 exiting the evaporator-heat exchanger 34.

This mass flow can be changed and set its settings as desired, by use of the control device 44. More specifically, the desired amount of steam coming in the circulating stream 38, taking into account the most contaminated incoming flows is less than 10% fraction of steam. The steam generated in the stream 38 is equivalent in weight to the amount recovered as distillate at position 100. Steam generated in the evaporation heat exchanger 34, despite the fact that its mass fraction is very small (about 1 to 10% of the circulating mass), absorbs the greatest amount of heat transferred from the condensing side of the evaporator 34. The choice of the number pair and the circulation rate of the concentrate is an important factor to reduce clogging and fouling, as well as prevent an excessive concentration of the fluid in the heat exchanger. Largely this parameter is most important to establish a very low high temperature for the circulating concentrate fluid to maintain an effective average of the logarithmic values of the temperature differential without crossing the temperatures in the evaporator-heat exchanger 34. Any temperature rise very quickly removes the specified value of temperature differential and heat transfer stops.

For example, if the pressure of the circulating concentrate was increased in the evaporator so that the fluid could not have formed some of the steam, the temperature will rise due to the absorption of heat up until there will not be an average logarithmic value of the temperature differential or thermal effect and, thus, the heat transfer will be reduced. Designed to reverse the pressure of the circulating concentrate system, consisting of a loss of static pressure and pressure losses due to friction was minimal. Actually, back pressure, first of all, is the loss of static pressure in a vertical heat exchanger, whereas the dynamic pressure drop of the heat exchanger is minimized. The flow of the circulating concentrate is then taken to obtain from about 1% to 10% fraction of steam in the output pipe 338. The resulting temperature rise is extremely low, and the specified average value of the temperature differential remains at the current level..

Figure 3 illustrates an embodiment of the invention, where a rich exhaust water vapor combines with the compressed water vapor to absorb the waste heat energy in a single evaporator 34. United pairs condense with the formation of the condensed distillate. If the existing pressure exhaust steam is incompatible or cannot be made compatible, in this case, provide a separate loop circoviridae concentrate and evaporators heat exchangers specifically designed to match each heat source. In addition, if waste heat is available only through condensible heat transfer fluid, then the exchange of waste heat expect to extract heat from the transporting fluid without the condensed distillate. A key feature of the design of the evaporator must always be its ability to maintain this favorable ratio of liquid mass and the mass of the pair, to create a vapor fraction from 1% to 10% in the evaporated fluid.

Figure 4 shows another diagram of a method, which enables regulation otvarennogo stream 24 from the heated separator 20 as long as the total effect concentration or concentration ratio of the system will not lead to the formation of supersaturated concentrate in relation to one or more components, which causes their deposition. While solids are formed and accumulate in a heated separator 20, otmerenny stream 24 is passed through the device 50 of the separation of solids and liquids for the removal of solids or sludge. In an alternative embodiment, the device 50 of the separation of solids and liquids can be placed between the pump evaporator 42 and the heat exchanger 34, the path of flow or in the General arrangement of equipment for processing stream. The recovered liquid is then recyclery back into the heated separator 20, as shown by the position 52, and the portion representing the number otvarennogo stream then passed through a heater 26 for heating and cooled to about 3° F (-16° C) stream 175. The device 50 of the separation of solids and liquids can be in any form known to experts in the art, such as a filter, hydrocyclone, centrifugal separator, gravity separator, a centrifuge, a decanter. This method is particularly preferred, when the main task is the extraction of the compounds in the form of solids, or when such connection has significant commercial value.

Figure 5 presents another embodiment of the method, by which the flow of steam may contain specific contaminants from the incoming stream. The heated separator 20 equipped with a fractionation column 54, which is located before the compressor 32 and the pipe 46 for the excess water vapor. The column 54 is used for fractionation and leaching contaminants using multiple stages in combination with reverse flow 56 clean cold water. Reverse flow can be deduced either from the input or from the exit stream of the device 18 pre-heating, or combinations thereof depending on the desired temperature of the return flow. This variant of the method is especially attractive when the incoming stream contains, for example, volatile substances, such as hydrocarbons, glycols, ammonia, amines, etc.

6 illustrates a typical pressure ratio and temperature of the various streams around the evaporative part of the way. For this discussion were made by different links, starting with a 2 by 4. Although the specific parameters of the process represented by example, they can be modified to meet any specific applications for distillation. The figure schematically presents conditions depending on the fluid, where the boiling point is not increased and the heated separator 20 is open at a pressure slightly above atmospheric, 16 psi(abs) (1.125 kg/cm 2 ) and 212,5° F (100,28°). Temperature rise of the circulating concentrate is 1° F for the pressure drop of the evaporator 2.5 psi (0,176 kg/cm 2 ). The vapor fraction of the circulating flow is about 10%.

Conditions around the evaporator-heat exchanger 34 can be represented in the form of the curve of evaporation or condensation, as shown in Fig.7. On the condensing side of the heat exchanger superheated vapor from the compressor at point C1 at a temperature of 289° F (142,78° C) and pressure 21,0 psi(abs) (1,477 kg/cm 2 ) connects with a rich stream of source of waste heat at the point C2 and condenses when the saturated vapor at point C’, about 232° F (111,11° (C) and 21.0 psi(abs) (1,477 kg/cm 2 ). This area is usually called the zone of lowering the temperature of superheated steam, and it consists of 2% of the surface area of the heat exchanger, the rest of the area is square, which releases the latent heat of condensation. Size reduction of the superheated steam temperature decreases with increase of the ratio of saturated waste heat to the compressed pair. A small decrease of pressure and temperature on the heat exchanger 34 is due to the characteristic of the heat exchanger pressure drop. Conditions to get the following: about 231,8° F (111° C) and 20.9 psi (1,47 kg/cm 2 ). The surface temperature on the condenser side is less than the saturation temperature of the incoming steam, education, thus, the film of condensate on the surface of dellamonica. Heat transfer, therefore, occurs due to the wet condition of the wall that supports effective temperature of the film at a saturation temperature of steam. The distillate is drained from the heat exchanger to the receiver capacitor 36 at point D, supporting the evaporator is free from liquid and providing the entire surface of the heat exchanger for condensation..

On vyparivaya side of the concentrate enters the heat exchanger countercurrent to the bottom at point a at a temperature of about 212, 5° F (100,28° (C) and the pressure of 18.0 psi(abs) (1,266 kg/cm 2 ) after the circulation pump 42. The speed of circulation is adjusted so that the speed of circulation of the mass of the concentrate was 10 times higher than the rate of steam. The temperature of a fluid mass of concentrate begins to rise to the point A’, and then flattens out for about 213,2° F (100,7° (C) when you reach a point where the hydrostatic pressure is overcome and the pressure is reduced to 15.5 psi(abs) (1,08 kg/cm 2 ). With the rise of concentrate in the heat exchanger 34 begins the formation of a pair under the influence of forced convection with the absorption of the transmitted latent heat. By increasing the mass of the fluid on vyparivaya side until the ratio of circulating mass and the mass of the pair reaches the desired limits, the effect of boiling is controlled within a forced convection and parcel stable nucleate boiling. Due to the large mass of the fluid flow, heat transfer surface is soaked at a temperature equal to the saturation temperature of the newly formed pair. With additional collateral flow rate (QA -1 ) for heat exchanger below 6000 BTU h -1 ft -2 (162750 kcal/m 2 · h) temperature rise at vyparivaya side can be maintained at a level less than 1° F maintaining a wet layer on the surface, by eliminating this risk of scale formation.

If the flow rate is too high, the instantaneous pressure drop due to the acceleration of vaporization temporarily exceeds the available static pressure, resulting in unstable temporary reverse current and possible damage to the wetted heat transfer surface. This can lead to clogging of the heat transfer surface. When the rate of heat flow below 6000 BTU h -1 ft -2 (162750 kcal/m 2 · h) and the ratio of the mass of the circulating concentrate the mass of the pair is less than 300, there is a region where the liquid and vapor can coexist in a stable system operation by maintaining the surface of the heat exchanger on vyparivaya part of the evaporator is fully moistened, without any risk of clogging or fouling.. Reference points A-D are also available on Fig.

Fig illustrates a vertical section of highly efficient heat exchanger 34, known to specialists as plate-frame heat exchanger, in which a series of vertically stacked plates with gaskets 60 are located between two continuous frames 62, 64. Such devices are well known due to their small size and the ability to have very high values of U or the overall heat-transfer coefficients. This type of heat exchanger having a configuration that enables one pass with a counter, is very well suited to the present invention offers the following advantages when implementing the present invention.

1. The heat exchanger plate type offers low fixed static pressure and very low pressure drop in the circulating concentrate fluid or vyparivaya side, while providing a relatively high heat transfer coefficient.

2. Heat flow can be easily adjusted by adding more space or plates in a given part of the frame.

3. Condensing side plate-frame construction is freely drained and has a low pressure drop, while maintaining a relatively high heat transfer coefficient.

4. Highly efficient heat transfer coefficient allows surface temperatures very close to the temperatures of both streams of fluid, reducing the risk of clogging.

5. High turbulence and equivalent high speed of the fluid flow to provide low clogging and maintain solid homogeneous suspended as they pass through the heat exchanger.

6. No hot or cold spots and no areas with a fixed flow inherent in the plate-in-frame design that reduces the risk of clogging or fouling.

7. The plates are smooth and well rounded, which reduces the risk of clogging.

8. The short residence time of the fluid reduces the risk of sediment because there is not enough time to reach equilibrium and education form the scum of pollutants.

In General, the heat exchanger plate type is very compact, and it is economical with plates made of a special alloy, which is resistant to the called fluid medium corrosion and stress corrosion cracking under stress, which is typical for applications of this type, when remove the salt. Other heat exchangers, type of pipe in the shell, pipe in pipe, type finned tubes, spiral type, can also be treated by specialists, subject to the specific requirements of the present invention.

Fig.9 is a graph of the dependence of the mass flow of the circulating concentrate and mass flow of steam, illustrating the preferred ratios calculated, generally designated 66. The desired range of 10 to 100 provides the fraction of steam from under 10% to about 1%.

Figure 10 presents a graph showing the effect on the local concentration coefficient (QC) QC heat exchanger depending on the risk of further supersaturation and sediment within the heat exchanger. The concentration ratio of the system can be expressed in the following General equation:

QC Society. =QC viperinae thread · QC heat exchanger

Concentration, reaching a steady state in a heated separator will cause permanent destruction of the pair in balance with continuous tarannum flow of the heated separator. The value of QC Society. typically of the order of less than 5 to about 20 times, depending on the level and type of contaminants in the incoming flow. Also, depending on the level of the mass of the vapor leaving the evaporator, determine the resulting QC heat exchanger (between 1.0 and 1.1) and the speed of the evaporated flow is adjusted so that the evaporator does not exceed the desired concentration levels. A typical example is shown below:

The ow contains 20000 solid solute and preferably, the concentrate was not more than 100000 solid solute.

Determined that the most effective mass ratio is 20, which gives a 5% fraction of steam, based on Fig.7.

QC heat exchanger , certain of Fig, is 1.07. It is calculated that QC total (100000/20000)=5.

It is calculated that QC evaporated flow rate (5/1,07)=4,7.

Therefore, the adjusted rate of the evaporated flow should be (1/4,7)=21% of the incoming stream.

Therefore, by using the method of vapor recompression and retrieve the waste of energy in combination with heat transfer with forced convection stage and keeping a careful selection of the ratio of the mass flow of the circulating system to the mass of the steam flow so that it is less than 300 to about 2, more specifically the ratio of from about 10 to 100, selection of heat flow less than 600 BTU h -1 ft -2 (1627,5 kcal/m 2 · h), and regulation of the evaporated flow to achieve the desired concentration coefficient, the result is a highly effective installation of water distillation, which is not subject clogging or fouling for a long period of operation. By combining two well-known schemes ways and enable schema extract waste heat from the unique configuration of the heat transfer and, more specifically, by calculating the specific relationship of circulating concentrate that was not mentioned in the prior art, the present invention provides an efficient way to distillatory water so that it does not contain impurities, without the risk of clogging or fouling.

The following examples serve to illustrate the invention.

EXAMPLE 1

This is cited as an example of the calculation is a means of showing the heat balance around the evaporator-heat exchanger. The example is calculated based installation distillation, designed to extract 53,000 US gallons per day (200622 liters) of pure distillate from the contaminated source.

Data exchanger:

The surface area of 3200 ft 2 (2973 m 2 )

Type - Plate-in-frame with

U - 542 BTU h -1 ft -2 F -1 (2637

kcal/m 2· h)

Adjusted average logarithmic value of the temperature differential - the 10.40° F

The calculated mode - (3,200)· (542)· (the 10.40); 18041224 BTU hour -1 ; (454638 kcal/h)

Calculated heat flux- (18041224)/(3200); 5638 BTU h -1 ft -2 ; (15190 kcal/m 2 · h)

Condensing side

Conditions on the input - 289° F 21,0 psi (abs) (superheated) (142,78° at 1.5 kg/cm 2 )

Conditions at the exit - 231,8° F 20,9 psi (abs) (111° s at 1.4 kg/cm 2 )

The saturation temperature at condensation - 232,0° F 21,0 psi (abs) (111,11° at 1.5 kg/cm 2 )

The latent heat of condensation - 957,4 BTU lb -1 (531 kcal/kg) at 21,0 psi (abs) (1.5 kg/cm 2 )

The flux of water vapor - 36.7 per US gallon per minute =18352 lb h -1 (8331,8 kg/h)

Q lowering the temperature of superheated steam - (18352)· (0,45)· (289-232) 471131 BTU h -1

Q-condensing - (18041224-471131); 17570093 BTU h -1 (4427663 kcal/h)

The calculated flow- (17570093)/(957,4); 18352 lb h -1 (8331,8 kg/h)

Viparyayah side

Conditions on the input - 212,2° F 18,0 psi (abs) (100° at 1.27 kg/cm 2 )

Conditions at the exit - 213,6° F to 15.5 psi (abs) (100,5° when 1,08 kg/cm 2 )

The latent heat of vaporization - 968,9 BTU h -1 at a 15.5 psi (243 kcal/h)

The ratio of circulating

mass to the mass of the pair - 10

The speed of the circulating concentrate - 370 US gallons per minute(1400 l/min) 184926 lb h -1

Steam flow - 18352 lb h -1 (8331,8 kg/h)

The percentage of pair - (18352/184926)=10%

Q evaporation (18352)· (968,9); 17782238 BTU h -1 (4481124 kcal/h)

Q found - (18492 6)· (1,0)· (213,6-212,2); 258896 BTU h -1 (65242 kcal/h)

Q General- (17782328)+(258896); 18041224 BTU h -1 (4546388 kcal/h)

This example shows that the vapor fraction of 10%, formed in the circulating fluid, captures 99% of heat transferred from the condensing side, and raises the temperature of the circulating fluid medium for about 1° F, even if it is 10 times less than the mass of the circulating fluid.

EXAMPLE 2

Installation of this type was made in the calculation of the restoration of 10,000 US gallons (37853 l) per day of pure distillate from subject to visalian flow from a well-educated on the land of the lagoon. The installation was tested over a long period of time and during this period were collected detailed data of testing. Pilot plant operated successfully for four months and when checking for a blockage in the evaporator and the separator was negligible. The equipment used in the pilot test included blower-compressor Spencer TM model GF36204E providing a differential pressure of 3.0 psi. During the test used a plate-frame heat exchangers with one standard passage.

Characteristics containing salt of an incoming stream of concentrated otvarennogo stream and processed the exit stream were as follows:

Note (1) - regulation of the pH before treatment to control ammonia.

Note (2) - presents the average values for the period of testing.

The output stream is of such quality that it can be unloaded in the ground water surface, because its quality exceeds all the requirements. The power consumption of the compressor was measured and recorded in various aspects of work, including lowering power and recycling. The measured power consumption is presented graphically in Figure 10 in the form of energy consumption per 1000 US gallons (3785,3 l) for different streams of distillate. Curve test data have been adjusted for the inefficiency of the compressor for some threads, and it was obtained the value of the uniform energy consumption 50 KW· h/1000 US gallons. In the calculation of the standard compressor efficiency 77% of the required energy consumption for installing high-efficiency distillation is about 65 kW· h/1000 US gallons. The amount of the evaporated flux is on average 10% of the incoming flow over the test period, which gives the average concentration coefficient (SC), equal to 10. After testing by visual observation showed no signs of scale formation in hot separator and the evaporator.

On Fig presents another variant of the present invention. In this embodiment, superheated otmerenny stream of saturated salt solution 140 take from preseparator 130 figure 1 and transmit high-performance installation 180 distillation of water.

Otmerenny stream 140 is subjected to instantaneous evaporation in the separator 200 low pressure to form stream 203 waste energy low pressure (typically 10-50 psig)(0,703-3,515 kg/cm 2 ) and concentrated otvarennogo stream 235 low pressure. Stream 203 waste of energy passed through the evaporator-heat exchanger 205, condensed to distilled water and collected in a surge tank 215.

Concentrated evaporated stream 235 high pressure is subjected to heat exchange with 240 for preheating water reservoir 175 with getting 245. The cooled concentrated otmerenny flow release to eliminate waste in the form of a stream 185. Waste energy 203 from the stream passed circulating the concentrate from the heated separator, where by controlling the relationship of circulating mass to the steam flow so that it ranged from less than 300 to about 1, less than 50% of a couple, or more precisely, less than 10% of steam is formed in the circulating flow of the concentrate leaving the evaporator 230. The vapor formed in the circulating flow, absorbs latent heat of vaporization, at the same time preventing the rise of temperature in the circulating concentrate for more than 1° F, maintaining the effective average of the logarithmic values of the temperature differential without crossing the temperatures in the evaporator-heat exchanger 205.

Recirculating the concentrate is removed at a controlled speed at position 265 with a pump 270 and replace at position 243 part supplied water reservoir 241. The heated portion of the formation water 244 again connect with the main amount of heated water reservoir 245 before entering the heated separator 250.

If the amount of waste energy 203 for a particular oil wells less than what is needed for distillation stream 245 of produced water that must be cleaned, in this case is provided by a separate circuit including the compressor 305 and the evaporator 315. If the same ratio of circulating mass to the steam flow of less than 300 to about 2, less than 50% of steam, or, more specifically, less than 10% of steam is formed in the circulating flow of the concentrate leaving the evaporator 350.

Excess water vapor produced from the heated separator 250, usually condense using an external capacitor 355. Energy can be converted to accumulation of heat or heat in other processes where it is appropriate. Threads 320, 360 condensed water collected in the equalization tanks 325, 365 condensate, and then combine using pumps 220, 330, 375 for the education of the incoming recycle stream of distilled water for steam generator 125. Using the above method you can get the regeneration water more than 85%.

If condensation occurring in the streams 210, 320, 360, formed non-condensable volatile matter, in this case pairs can be automatically released by means 217, 335 and 370, respectively.

Working pressure and corresponding temperature of the heated separator is chosen in a wide range from full vacuum to less than 50 psi (3,515 kg/cm2 ), more typically, the pressure is chosen slightly above or below atmospheric, 12 psi (abs) (services, 0.844 kg/cm 2 ) vacuum to overpressure of 2 psi (0,141 kg/cm 2 ).

On Fig presents another embodiment of the present invention. In this embodiment, the energy part 202 of waste heat from position 200, and/or excess water vapor 255 is used as an energy source for mold 405 by means of the heat exchanger 400 and schemes pumping 415, 420. The crystallizer operates under boiling at a temperature at least 10° F, and most preferably, from 20° F to 30° F lower than the temperature of the water vapor from the heated separator 250. The mold can operate at a pressure equal to, above or below atmospheric pressure. When the amount of energy in the flow of waste energy 202 and/or redundant pair 255 exceeds the amount necessary for the operation of the mold, then it is possible to carry out the condensation with external condensing means.

Concentrated otmerenny stream 275 and heated to separate the concentrate stream 265 serves to supply the crystallizer tank 280. Nearly saturated salt solution is passed through the feed pump 425 in the circulating loop of the mold 410. Slip stream of the circulating suspension at position 410 is removed by means of a pump 435 and passed through the device 440 separating solids and liquids, or directly transferred to the pond for evaporation. A typical device for separating solids and liquids, known to the specialists in the art, may include a filter, filter press, gravity settling tank, clarifier, a cyclone separator, a decanter and centrifuge.

The filtrate 450 recyclery to supply the crystallizer tank 280. The solid material 445 leaving the separator 440 solids and liquids collect in suitable media for storage and transported to the elimination of waste. Any excess containing impurities water collected in storage areas 455 or in the pool for evaporation, can be recycled by means of pump 460 back to supply the crystallizer tank 280.

The condensed water flows 210, 407, 490, you can collect and combine to produce the recirculated stream of distilled water for supply to the steam generator 125. When using the above method achieves 100%water recycling and zero discharge.

As for equipment, which is used in this system, the experts in this field will easily determine which of the heated separators, heaters, evaporators, pumps, compressors/blowers, molds, etc. it is better to use. May be approved by the other modifications without departure from the substance and scope of the invention.

Although embodiments of the invention have been described above, it is not limited, and specialists will be clear that various modifications form part of the present invention, if they are not a retreat from the idea, the essence and scope of the claimed and described invention.

1. The method of obtaining energy for treatment of water used in the extraction of crude oil from oil-bearing formation containing crude oil and water, characterized in that it contains the following stages:

2. The method according to claim 1, characterized in that the heat energy contained in the liquid fraction, received and used for water distillation.

3. The method according to claim 1, characterized in that the heat energy contained in the vapor fraction, received and used for water distillation.

4. The method according to claim 1, characterized in that the lower pressure of crude oil, produced water and steam produced from oil-bearing stratum, in this case, thermal energy is derived from the fraction of steam instantaneous evaporation, and the resulting energy is used for water distillation.

5. The method according to claim 1, characterized in that the crude oil and the liquid fraction separated in the separator of oil and water.

6. The method according to claim 1, characterized in that the incoming water flow condition prior to its contacting with steam.

7. The method according to claim 2, characterized in that the incoming water flow condition to remove mineral impurities.

8. The method according to claim 1, characterized in that the crude oil from step C) has a density of from 7° to 20° on the scale of the American petroleum Institute.

9. The method according to claim 1, characterized in that the incoming water stream contains ground water or produced water.

10. The method according to claim 1, characterized in that it further receive thermal energy contained in the liquid fraction and a vapor fraction, and use thermal energy for water distillation.

11. The method according to claim 10, characterized in that it further treated produced water by distillation water.

12. The method according to claim 1, characterized in that additionally use the heat exchanger for receiving at least part of thermal energy in the liquid fraction.

13. The method according to item 12, characterized in that it further heat the incoming water flow through at least part of the energy received from the heat exchanger.

14. The method according to claim 1, characterized in that the crude oil includes gravity drainage extraction using steam or cyclic steam stimulation or pushing of steam and gas.

15. The method of obtaining energy from the equipment for the extraction of crude oil contained in the oil-bearing formation in which the energy for water treatment obtained when the extraction of crude oil, while this method differs in that it contains the following stages:

16. The method of obtaining energy for treatment of water used in the extraction of crude oil from oil-bearing formation containing crude oil and water, comprising the following stages:

17. The method according to item 16, characterized in that thermal energy from the stage g) is obtained from the fraction of steam, and optionally provide a recirculation of the excess thermal energy from thermal energy obtained from the fraction of steam at stage g), for injection into the reservoir.

18. The method according to item 16, characterized in that in stage (e) get couples together with crude oil and formation water from oil-bearing stratum and additionally provide instant vaporization of steam in the degassing separator, and heat energy on stage W) is selectively obtained from the pair, and additionally carry out storage, air-conditioned and distilled water from the installation of distillation.

19. The method according to item 16, wherein the incoming stream of water contains ground water or produced water.

20. The method according to item 16, characterized in that the use of heat exchange means and teploperenosu environment for transferring the received heat to the installation of distillation.

21. The method according to item 16, characterized in that the crude oil has a density of from 7 to 20° on the scale of the American petroleum Institute.

22. The method according to item 16, wherein the crude oil comprises gravity drainage extraction using steam or cyclic steam stimulation or pushing of steam and gas.

23. The method according to item 16, characterized in that thermal energy on stage W) is obtained from the fraction of steam, and the pressure of the vapor fraction exceeds the pressure required for injection into the reservoir.

24. The method according to 17, characterized in that the fraction of steam has a pressure suitable for injection into the reservoir.

25. The method according to item 23, wherein the pressure of the vapor fraction in the range of 1900 to 2400 pounds per square inch.

26. The method according to paragraph 24, wherein the pressure of the vapor fraction in the range from 1200 to 1700 psig.

27. The method according to item 16, characterized in that thermal energy is derived from the fraction of the liquid and served in a heat exchanger to heat the incoming fluid flow.

28. The method of obtaining energy in the processing of crude oil for processing water obtained during the extraction of crude oil, characterized in that it contains the following stages:

29. The method according to p, wherein selectively use the compressor for condensing part of the faction pair up with distilled water when the quantity of waste energy is sufficient for the heated separator.

30. The method according to p, characterized in that the missing fraction of steam in the crystallizer solids to extract the energy contained in the vapor fraction to form a solid contaminants in the mould of non-volatile compounds present in the concentrated liquid fraction containing the impurities.

31. The method according to p, characterized in that the missing fraction of steam in the external condenser to condense vapor into liquid.

32. The method according to p, characterized in that the amount of waste water containing impurities, processed in this way is equivalent to the amount of waste energy obtained by this method.

33. The method according to p, characterized in that the incoming stream is pre-treated before preheating.

34. The method according to p, wherein the pre-processing thread is filtration, or ion exchange, or gravity separation, or chemical treatment, or steaming.

35. The method according to p, characterized in that it further carry out the subsequent processing of the condensed distillate.

36. The method according to p, characterized in that subsequent treatment is filtration, or ion exchange, or advanced oxidation or adsorption, or aeration.

37. The method according to p, characterized in that the mass contains about 10 wt.% the concentration of steam.

38. The method according to p, characterized in that the steam condenses in the heat exchanger plate type.

39. The method of obtaining energy in the processing of crude oil for processing water obtained during the extraction of crude oil, characterized in that it contains the following stages:

40. The method of obtaining energy in the processing of crude oil for processing water obtained during the extraction of crude oil, characterized in that it contains the following stages: