EA004424B1 - Method of removing water and contaminants from crude oil containing same - Google Patents

Abstract

1. A method of removing water from crude oil containing water, comprising of steps of: a) providing a source of crude oil containing water to a dehydrator for dehydrating said crude oil containing water, said dehydrator having an inlet and an outlet at temperatures sufficient to vaporize water from said surface; b) exposing said source of crude oil to said dry crude oil; c) vaporizing at least a portion of water in said source; and d) re-circulating at least a portion of dehydrated crude oil for contact with at least one of said dehydrator or said source of crude oil for maintaining a substantially uniform temperature at said vaporizing surface. 2. The method as defined in Claim 1, wherein said temperature is a flash evaporating temperature for water. 3. The method as defined in Claim 1, including pre-conditioning said source for removal of solids and minerals. 4. The method as defined in Claim 1, including pre-conditioning with separation means for separating said solids and minerals from said source crude oil. 5. The method as defined in Claim 1, further including the step of collecting gaseous components from said vaporizing and condensing said components. 6. The method as defined in Claim 1, further including the step of regulating heat content of said dehydrated crude oil re-circulated with heating means. 7. The method as defined in Claim 1, wherein said source of said dry crude oil has an API index of between 7 degree API and 20 degree API. 8. The method as defined in Claim 1, wherein in said dehydrated crude oil has a basic sediment water content of less than 0.5% by volume water. 9. The method as defined in Claim 1, wherein said source of crude oil contains greater than 5% by volume water. 10. The method as defined in Claim 1, further including step of collecting and condensing vaporized water. 11. The method as defined in Claim 1, further including a step of collecting and condensing light hydrocarbon fluid. 12. The method as defined in Claim 10, farther including the step of purifying said condensed water. 13. The method as defined in Claim 10, further including the step of re-circulating condensed light hydrocarbon fluid to said source of crude oil. 14. The method as defined in Claim 11, further including the step of diluting said source of crude oil with condensed light hydrocarbon fluid. 15. A method of removing water from crude oil containing water, comprising of steps of: a). maintaining a temperature at an inlet and an outlet sufficient to vaporize water from said surface; b) contacting said source and said dry crude oil to flash water from said source to thereby remove said water from said source; and d) selectively heating said surface of said dry crude oil to return heat energy lost from flash evaporating water from said source. 16. The method as defined in Claim 15, wherein said heating is provided by at least one of re-circulating dehydrated crude oil into said dry crude oil and re-circulating dry dehydrated crude oil into contact with said source of crude oil. 17. The method as defined in Claim 15, wherein prior to step b), said source is pre-conditioned. 18. The method as defined in Claim 17, wherein in pre-conditioning includes removal of solid and mineral from said source. 19. A method of removing water from crude oil containing water, comprising of steps of: a) providing a source of crude oil containing water to a dehydrator for dehydrating said crude oil containing water, said dehydrator having an inlet and an outlet and a vaporizing surface of dry crude oil at a temperature sufficient to vaporize water contacting said surface; b) pre-washing said source of crude oil containing water to remove alkali metals and alkaline earth metals; c) separating said alkali metals and said alkaline earth metals and oil in a preliminary separation step; d) passing washed oil into said dehydrator to flash evaporate water from said washed oil to remove water therefrom; e) selectively pre-heating crude oil to be treated in said dehydrator with treated dehydrated crude oil from said dehydrator to return heat energy lost from flash evaporating water; and f) maintaining a uniform surface temperature. 20. The method as defined in Claim 17, further including the step of collecting gaseous vapors evolving from said dehydrator. 21. The method as defined in Claim 17, further including the step of collecting light hydrocarbon liquids formed during dehydration. 22. The method as defined in Claim 17, wherein separated minerals are collected in a concentrated brine.

Description

Field of Invention

The present invention is directed to an improvement of a method for dehydration of crude oil and a device for this, and more specifically, the present invention relates to a method of dehydration of crude oil, which can overcome the problems associated with the instability encountered in currently used methods and devices for processing heavy oil streams with high water content, provides improved methods for supplying thermal energy and extraction and removal of suspended and dissolved compounds from the input stream.

BACKGROUND OF THE INVENTION

In many regions of the world, heavy oil, a hydrocarbon material having a much higher viscosity or lower density in degrees ΑΡΙ - American Petroleum Institute (less than 20 ° ΑΡΙ, usually from 7 to 12 ° AP1) - than ordinary crude oil , economically profitable for commercial sale. During the production process and before being transported to refineries, in order to improve the quality, heavy oil is pretreated for dewatering and removal of suspended solids, so that, as a rule, a basic sediment and water content (B 8 & XV) of less than 0.5 is achieved vol.%, and chloride content, less than 30 parts per million (weight). The water content of the treated heavy oil should typically be 0.3 vol.% Or less.

Conventional methods for refining crude oil were shown to be ineffective with respect to heavy oil until US Pat. No. 33999, C1a1 C1 A1, issued July 21, 1992, and Canadian Patent 1302937, C1a1 C1 A1, issued June 9, 1992 of the year. These patents describe a simple device that can be placed away from oil production sites for dehydration of heavy oil with a low risk of foaming and unstable operation, while continuously producing dehydrated oil that exceeds the required parameters in quality. These water separators have been found to be limited when applied with a water content in the oil inlet stream of less than 5%, and are sensitive to foaming and process instability with large inlet water flows. Despite the fact that the work of several of these water separators implementing the technology of the mentioned patents 33999 and 1302937 is known, areas have been discovered for improvements necessary to overcome the restrictions on the water content in the oil input stream and on unstable operation caused by interruptions in the pre-treatment.

In addition, additional problems were discovered with previously used devices, in which, although they dehydrated heavy oil, the processed oil still contained high concentrations of suspended solids, such as clay and silica, and dissolved compounds, such as chlorides. These undesired compounds continue to pose many problems in pipeline systems for transporting oil and in refining equipment to such an extent that significantly reduces the commercial attractiveness of heavy oil.

Accordingly, one of the objectives of the present invention is to achieve success in overcoming the limitations encountered in previously used equipment.

SUMMARY OF THE INVENTION

One of the objectives of the present invention is the creation of a dehydrated crude oil recycled stream bypassing the water separator to mix with the input stream to reduce the ratio of residual water and oil in the mixture in contact with the surface of the oil in the water separator, thereby making it possible to have a higher water content in the crude oil while maintaining the stability of dehydration operations.

Another objective of one of the embodiments of the present invention is to provide a method for dehydration of crude oil containing water, comprising the following stages:

a) providing a source of crude oil containing water;

b) providing a water separator for dehydration of crude oil containing water, the water separator has an inlet and outlet and an evaporation surface for the dehydrated crude oil at temperatures sufficient to evaporate water in contact with this surface;

c) introducing crude dehydrated oil into a source of crude oil;

ά) evaporation of water in the source; and

e) recycling at least a portion of the dehydrated crude oil to contact at least one device from the group of a water stripper or source of crude oil to maintain a substantially uniform evaporation surface temperature.

Conveniently, when at least a portion of the recirculated dehydrated crude oil stream near the water separator is introduced into the water separator and distributed below the surface of the hot crude oil in the water separator, the corresponding temperature is maintained equal to or above the evaporation temperature of water, and on the oil surface or below it, and in the whole contained oil, thereby providing a means to reduce the risk of interruptions in the process and instability due to foaming.

A further object of the present invention is to provide a recycled stream of dehydrated crude oil bypassing the water stripper for mixing with the inlet stream to make it possible to supply additional heat energy (external or waste heat energy) or to extract heat energy from the water stripper to obtain an energy-efficient and balanced process.

Another objective of the present invention is to provide a method for dehydration of crude oil containing water, comprising the following stages:

a) providing a source of crude oil containing water;

b) providing a water separator for dehydration of crude oil containing water, the water separator has an inlet and outlet and an evaporation surface for the dehydrated crude oil at temperatures sufficient to evaporate water in contact with this surface;

c) contacting the source and the dehydrated crude oil for explosive evaporation of water from the source, thereby removing water from the source; and

b) selective heating of the surface of the dehydrated crude oil to compensate for the loss of thermal energy during explosive evaporation of water from the source.

The surface of the dehydrated crude oil may be selectively heated by reintroducing the dehydrated crude oil, auxiliary heat supply and the like. An important aspect is that the heat used for evaporation is recovered in such a way that a uniform or substantially uniform surface temperature is maintained. This is one of the important work parameters that must be supported.

A further objective of the present invention is to provide means for removing suspended solids accumulated in the contained dehydrated crude oil, introduced by a source of oil or obtained during the dehydration process.

Particulate matter suspended in a recirculated dehydrated crude oil stream can be removed using continuous or loading separators to prevent sludge formation, blockage, and other complications.

Another objective of the present invention is to rinse with water the original source of crude oil in combination with treatment in a water eliminator to remove soluble dissolved solids of impurities introduced into the crude oil in the source, and to create secondary water with low conductivity and pure dehydrated crude oil.

Prior to the present invention, the previously used methods with respect to dehydration of heavy oil had limitations associated with stability and risk of foaming, maximum water content or emulsion content in the inlet stream and heavy oil, and the level of chloride, clay and silica compounds in commercial dehydrated crude oil .

Another objective of one of the embodiments of the present invention is to provide a method for dehydration of crude oil containing water, comprising the following stages:

a) providing a source of crude oil containing water;

b) providing a water separator for dehydration of crude oil containing water, the water separator has an inlet and outlet, as well as an evaporation surface of the dehydrated crude oil at temperatures sufficient to evaporate water in contact with this surface;

c) pre-flushing the source of crude oil containing water to remove alkali metals and alkaline earth metals;

b) the separation of alkali metals and alkaline earth metals and oil at the preliminary stage of separation;

e) the passage of the washed oil through a water stripper for explosive evaporation of water from the washed oil to dehydrate it;

ί) selective preheating of crude oil intended for processing in a water separator using treated dehydrated crude oil from a water separator to compensate for heat energy losses during explosive evaporation of water; and

d) maintaining a uniform surface temperature.

Improvements are being developed to remove the restrictions imposed by the maximum water content in the input stream from a source of crude oil and to produce very clean and dehydrated heavy oil, a product relatively free of water, particulate matter and chlorides.

The present invention relates to improvements of the method and to a device used for dehydration of crude oil containing water, including a housing, means for passing and distributing liquid crude oil in the casing and on the main surface of the dehydrated crude oil, means for controlling the level of crude oil and means for supplying thermal energy necessary to maintain liquid oil at a temperature equal to or higher than the distillation temperature to evaporate water and light hydrocarbon fractions.

The light hydrocarbon fractions and water leaving the housing are condensed by any suitable means known in the art and are collected and separated into water and light hydrocarbon fractions in the liquid phase. Any non-condensable vapors are released from the device for use by any safe means. Dehydrated crude oil that meets the requirements of B8 & for pipelines is pumped from the water stripper for transport to processing and further refining units.

Typically, a water stripper known in the art works well enough to produce dehydrated crude oil, however, there are several problems:

1. The water stripper has restrictions on the maximum water content in the input stream of crude oil (νε), on the ratio of water to oil, less than 10%, and more specifically νο, less than 5%, to reduce the risk of unstable operation with foaming tendencies. This necessitates the use of conventional treatment facilities installed in front of the water separator to reduce the water content in the original crude oil before introducing from 50-20% νο to less than 5% νο in the water separator.

2. The dehydrated crude oil leaving the water stripper has a high chloride content, which causes metallurgical and corrosion problems with the following processing units and transportation pipelines.

3. It was found that with explosive evaporation of water and with the effective removal of all emulsions, solid particles, such as clay and silicon dioxide compounds concentrated in the dehydrated oil phase, there is a tendency to sedimentation, clogging and / or damage to thermal elements.

4. In addition, it was found that the water stripper is sensitive to unstable operation and to trends in foaming, causing jumps in dehydration temperature and the production of oil containing water.

The present invention seeks to solve these problems by creating a methodology and device in order to exceed the performance of the water separator used previously in this field.

In one embodiment of the present invention, at least a portion of the dehydrated crude oil exiting the water separator is recycled and mixed with the crude oil inlet stream before being introduced into the water separator body. By increasing the recirculated flow, a suitable and stable composition with a predetermined water content at the inlet of the housing can be maintained to control the tendency to foam and to cause complications during operation. At higher values of the recirculated flow, the initial maximum levels of water content can be increased to stable levels in excess of 10% νο, and continuous stable operation is maintained. This eliminates the need for conventional processing before the water stripper and can eliminate interruptions in the process taking place in the water stripper if a pre-treatment device is used and this device fails.

An additional embodiment of the present invention requires that at least a portion of the recycled dehydrated crude oil is recycled and distributed directly below the evaporation surface of the dehydrated crude oil. This method maintains the surface temperature of the dehydrated oil in the water stripper equal to a temperature sufficient for explosive evaporation of water or exceeding it. Drops of water from the inlet stream are not allowed to penetrate the surface of the crude oil, thereby preventing cooling below the surface, and the destruction of the surface by foaming, and the unstable operation of the water stripper.

Advantageously, means for transporting external heat can be further added to the recycling circuit to control the exact temperature of the inlet stream to the water separator body. This improvement of the method will regulate the exact level of pre-dehydrated water boiling in the oil inlet stream to control the level of residual water in contact with the hot surface of the dehydrated oil. This stage should be used to prevent overcooling of the bath and to eliminate the effects of foaming caused by excessive destruction of the evaporation surface.

External heat exchangers can also be used to cool the input stream. They can be used if the input stream of the original crude oil already contains sufficient or excess thermal energy required for explosive evaporation or distillation of water vapor. Cooling the inlet stream can control the explosive evaporation operation and prevent complications in the process.

As an additional part, a solids / liquid separation device, examples of which include a filter, a hydrocyclone, centrifugal separators, density separators, a centrifuge, or any combination thereof and the like, can be used in the recycled flow circuit continuously or in a charging mode to remove suspended solids particles from hot dehydrated oil.

In addition, a clean water rinse chain may be added to the water purifier inlet stream to reduce the content of undesired dissolved compounds, such as chlorides, in dehydrated crude oil. The entire stream of contaminated water, or part thereof, is processed using an appropriate processing method to create a stream of pure water and a highly concentrated brine, suspension or solid product. Dehydrated clean water is recycled back to pre-treat the original crude oil. As a rule, water or any aqueous solution containing compounds to improve chloride extraction is most desirable; in another case, any regenerated liquid with appropriate aggressive solvent dissolving ability for chlorides can be considered.

Preferably, in addition to the dehydrated oil having a B 8 & content of less than 0.5% gf by volume, embodiments of the present invention, used in combination or separately, could produce a dehydrated pure crude oil substantially free of particulate matter containing less than 30 ppm (weight) of chlorides, with continuous and stable operation, with low risk of foaming and interruptions in the process. The oil obtained using this method is easily sold and most desirable, especially in the case of heavy crude oils with a density in the range from 7 to 20 ° AP1.

After thus describing the present invention, reference will hereinafter be made to the accompanying drawings, illustrating preferred embodiments.

Brief Description of the Drawings

FIG. 1 is a generalized block diagram that illustrates the recycling of dehydrated oil to the inlet stream of the water separator and to the water separator;

FIG. 2 is an additional generalized block diagram representing external heat transfer on a recycle to control the temperature of the inlet stream, or the surface of the water stripper, or both together;

FIG. 3 is an additional generalized block diagram representing a particulate / liquid separator for removing suspended solids; and FIG. 4 is a generalized block diagram illustrating the addition of washing water to remove dissolved compounds such as chlorides.

The same numbers used to refer to the drawings indicate like elements.

DETAILED DESCRIPTION OF PREFERRED EMBODIMENTS

Turning to FIG. 1, heavy oil with a density between 7 and 20 ° ΑΡΙ, indicated by number 10, usually contains a mixture of crude oil, water, an oil / water emulsion, dissolved compounds such as chlorides, and solid particles such as clay, metals and dioxides silicon. Crude oil, as a rule, is taken into a gravity separator, a heated or non-heated processing device 12, at a pressure from atmospheric pressure to

100 pounds per square inch (6.2 kg / sq. Cm). Heated cleaning devices, as a rule, operate at temperatures from 170 to 285 ° E (from 77 to 141 ° C). In purifiers, solid particles and the volume of hard water are separated and removed from the original crude oil at point 14. Maximum water contents, from less than 10% to, more typically 5 vol.%, Can be achieved in the input stream of the original crude oil 18, exiting the primary purifier through the valve assembly 20. The water stream 22 typically contains dissolved compounds, such as sodium chloride (5000 to 50,000 ppm (weight)) and silica, and suspended compounds, such as clay and sand.

The original crude oil with a maximum water content of about 5% in the form of an emulsion, free of free water, is introduced into the water separator 24, where the crude oil and emulsions are evenly distributed over the hot surface of the dehydrated crude oil (not shown), operating at a temperature equal to the temperature of water evaporation or higher. Water is explosively evaporated from the oil or removed by distillation, with water and low boiling hydrocarbon components leaving the oil through column 26 and passing through line 28. If desired, water and low boiling components can be sent to a condenser 30, and subsequently to a steam separator -liquid 32. Dehydrated crude oil with a higher boiling point is discharged from the water separator 24 through a pipe 34.

In the separator 32, water and the light hydrocarbon fraction are separated by the difference in specific gravity. Water is discharged through line 36 and pump 38. The light hydrocarbon fraction is transported from separator 32 via pump 40 through line 42 and can be removed for discharge at line 44 or at least partially recycled and mixed at the inlet with crude oil 10 via line 46 for dilution of incoming crude oil and, thereby, facilitating its further processing. Non-condensable, that is, light hydrocarbons, inert gases (nitrogen, carbon dioxide, hydrogen sulfide) are removed by a fan from the separator 32 and discharged or recovered using any suitable safe means.

As shown in FIG. 1, the dehydrated oil can be recycled at point 48 and recycled as a stream 50 for mixing with the input stream 18 before it is distributed on the surface of the hot oil in the water separator 24.

In order to maintain the temperature of the hot surface of the oil, at least a portion of the recycled stream 50 can be recycled directly to the water remover 24 and distributed on or directly below the surface of the hot dehydrated crude oil. It has been found that by recirculating the dehydrated crude oil to the inlet stream 18 and separately or in combination with recirculating the dehydrated crude oil to the surface of the hot bath by using stream 52 (dashed lines), the following important advantages can be obtained:

a) The water content in the original crude oil in stream 18 can be increased by more than 10% and even more than 20 vol.%. This increase means that the need for conventional processing, designated as 12, can be eliminated without the risk of process instability or foaming in the water separator.

b) If conventional primary treatment 12 is used, the recirculated flow can be used to rid the water trap of complications associated with instability or performance issues if the pre-treatment becomes unstable. This means that the commercial parameters of dehydrated crude oil are not at risk and recycle for non-standard commercial oil from commercial oil storage facilities and pipelines is excluded.

The recycle ratio at point 50 to the inlet stream may vary depending on the actual temperature, and the speed of the recycle stream 52, and the degree of conditioning of the inlet stream, and a decrease in the maximum water content required at the inlet of the water separator. Similarly, the ratio of the recycled stream 52 to the recycled stream 50 will vary for each application in order to balance the conditioning of the water purifier inlet stream and the surface temperature in the water purifier. Depending on the relative magnitude of the recycled oil stream 50 to the dehydrated commercial oil 34, common pumps or separate pumps can be used, as is known to those skilled in the art. Recycling 52 may also be provided with separate pumping facilities.

Turning to FIG. 2, an improvement in the recirculation of FIG. 1, where heat exchange means 54 are added to the recirculation circuit to condition the temperature for streams 56 and 52. Streams 56 and 52 can be heated or cooled to the same temperature or, independently, to different temperatures in order to establish the heat balance of the input stream and the bath surface hot crude oil. Any form of suitable heat source, such as direct heating tube furnaces, indirect heating tube furnaces, heat exchangers or heat removal or cooling devices, can be selected. An additional consideration regarding the temperature in streams 56 and 52 is whether the input stream comes from heated primary processing agents at a temperature of from 170 to 285 ° E (from 77 to 141 ° C) or from a reservoir for storing the original crude oil at a temperature of 60 up to 100 ° E (from 16 to 38 ° C).

FIG. 3 illustrates a further improvement for incorporating particulate / liquid separators 62 used to remove suspended solids, such as clay, sand and precipitated salts, from dehydrated crude oil. The solid / liquid separator 62 may be selected from any suitable suitable device known to those skilled in the art, such as gravity separators, clarifiers, filters, sieves, cyclones and centrifuges. The amount of recirculated flow from point 50 is selected so as to correspond to the operating range of the particulate / liquid separator 62, and is specifically selected so as to correspond to the rate of dewatering of solid particles at point 64 greater than or equal to the content of solid particles entering the water separator 24 at point 18 and produced during dehydration.

Particulate matter can be removed on a continuous or loading basis and, above all, provides an opportunity for the onset of particulate matter to be removed from the water separator 24 in order to prevent sedimentation and clogging. The formation of precipitation from solid products on the heating elements contained inside the device 24 or outside the device 24 is harmful to the performance of the elements and can be a problem in ensuring safe operation.

Returning to FIG. 4, the following variation of the invention is presented, representing the addition of water flushing agents in a water stripper to remove dissolved solids. The crude oil may contain high concentrations of sodium, calcium, magnesium, chlorides, sulfur, carbonates, silicon dioxide and the like. All of these compounds, especially chlorides, are currently undesirable in dehydrated oil as a commercial product and can have a significant commercial effect on the price of crude oil or even limit sales. Typically, refineries currently require less than 30 ppm chlorides in commercial crude oil (weight).

Using the improvement of FIG. 4, pure water 66 is injected and thoroughly mixed with the original crude oil 10 at point 68. The input mixture 10 passes through a primary treatment separator at point 12. The volume of water contaminated with brine is separated from the oil and discharged through a pipe 22 to the processing unit water 70.

The washed crude oil is discharged at point 18 and becomes an input stream to the water separator. The input stream can be conditioned either in the primary processing unit 12, or by using recycled streams 50 and 52 to ensure the stable operation of the water separator 24. The washed crude oil at point 18 contains significantly reduced levels of dissolved compounds, satisfying or exceeding the established requirements for commercial oil.

The water treatment scheme selected for each application should ensure that unwanted compounds in stream 22 are substantially removed to meet the process requirements for removal at point 18. Typical water treatment methods are microfiltration, reverse osmosis, distillation, flocculation, clarification, and coagulation.

The treated water 72 enters the equalization vessel for the treated water 74 and is transported by a pump 76 for re-injection at point 68 using the pipe 66.

As an optional feature, the water obtained by condensing the steam from the separator 32 can be transported directly by means of a pump 78 or to a treated water equalizing tank 74 using a pipe 80, or to a water treatment unit 70 using a pipe 82, if water treatment is desired. The entire stream of produced water can exit the separator 32 in stream 84 or from the water treatment unit 70 through stream 88. Additional fresh water can be introduced into the treated water storage tank 74 at point 90 if there is a water balance deficit.

Using the following improvements, independently or in combination, the process methods, as described in the present invention, result in dehydrated pure crude oil that meets or exceeds the new commercial requirements for commercial commerce.

Although embodiments of the present invention are described above, it is not limited thereto, and it will be apparent to those skilled in the art that numerous modifications form part of the present invention insofar as they do not deviate from the spirit, nature and scope of the description and claims of the present invention.

Claims (22)

CLAIM 1. The method of dehydration of crude oil containing water, comprising the following stages: a) the supply of crude oil containing water to a water separator for dehydration of crude oil containing water in a water separator having an inlet and outlet, at temperatures sufficient to evaporate water from the evaporation surface; b) introducing crude oil into said dehydrated crude oil; c) evaporating at least a portion of the water in the crude oil; and b) recycling at least a portion of the dehydrated crude oil to contact at least one water stripper and crude oil to maintain a substantially uniform evaporation surface temperature. 2. The method according to claim 1, where the specified temperature is the temperature of the explosive evaporation of water. 3. The method according to claim 1, comprising pre-conditioning the crude oil to remove particulate matter and minerals. 4. The method according to claim 1, comprising pre-conditioning using separation agents to separate said solid products and minerals from crude oil. 5. The method according to claim 1, further comprising the step of collecting gaseous components from said evaporation and condensing said components. 6. The method according to claim 1, further comprising the step of controlling the heat content of said dehydrated recycled crude oil using heating means. 7. The method according to claim 1, where the crude oil of the specified dehydrated crude oil has an index ΑΡΙ in the range between 7 and 20 ° ΑΡΙ. 8. The method according to claim 1, where the specified dehydrated crude oil has a basic content of sedimented water, less than 0.5 vol.% Water. 9. The method according to claim 1, where the crude oil contains water in an amount greater than 5 vol.%. 10. The method according to claim 1, further comprising the step of collecting and condensing the evaporated water. 11. The method according to claim 1, further comprising the step of collecting and condensing the liquid fraction of light hydrocarbons. 12. The method of claim 10, further comprising the step of purifying said condensed water. 13. The method of claim 10, further comprising the step of recycling the liquid fraction of light hydrocarbons to crude oil. 14. The method according to claim 11, further comprising the step of diluting the crude oil with a liquid containing a condensed fraction of light hydrocarbons. 15. The method of dehydration of crude oil containing water, comprising the following stages: a) maintaining an inlet and outlet temperature sufficient to evaporate water from the evaporation surface; b) contacting the crude and dehydrated crude oil for explosive evaporation of water from the crude oil, thereby removing water from the crude oil; and b) selective heating of the surface of the dehydrated crude oil to compensate for the loss of thermal energy during the explosive evaporation of water from crude oil. 16. The method of claim 15, wherein said heating is provided by at least one dehydrated crude oil recycling to said dehydrated crude oil and recycling of the dehydrated crude oil to contact with the crude oil. 17. The method according to clause 15, where before stage b) crude oil is pre-conditioned. 18. The method according to 17, where the pre-conditioning includes the removal of solid particles and minerals from crude oil. 19. A method of dehydration of crude oil containing water, comprising the following stages: FIG. one -t ---- CX1 * Liquid fraction of light hydrocarbons SDD crude oil FIG. 2 a) the supply of crude oil containing water to a water separator for dehydration of crude oil containing water in a water separator having an inlet and outlet, at temperatures sufficient to evaporate water from the evaporation surface; b) pre-flushing crude oil containing water to remove alkali metals and alkaline earth metals; c) separation of alkali metals and alkaline earth metals and oil in a preliminary separation step; b) the passage of the washed oil through a deoxidizer for explosive evaporation of water from the washed oil to dehydrate it; f) selective preheating of crude oil intended for processing in a water separator using treated dehydrated crude oil from a water separator to compensate for thermal energy losses during explosive evaporation of water; and 1) maintaining a uniform surface temperature. 20. The method of claim 17, further comprising the step of collecting gaseous vapors exiting said water stripper. 21. The method according to 17, further comprising the stage of collecting liquid fractions of light hydrocarbons formed during dehydration. 22. The method according to 17, where the separated minerals are collected in concentrated saline.