Removal of gaseous contaminants from gas flow containing gaseous contaminants and device to this end. RU patent 2520269.

FIELD: process engineering.

SUBSTANCE: invention relates to removal of gaseous contaminants from gas flow containing gaseous contaminants and device to this end. Stock gas flow is cooled to form suspension containing the solid contaminant, liquid-phase contaminant and gas phase enriched with methane. Suspension is fed to cryogenic separator (4) for gas phase (5) to be withdrawn therefrom. Said suspension is diluted by liquid-phase contaminator (6) and sucked into ejector (9) and therefrom in heat exchanger (10) arranged outside said separator and wherein sold contaminator is fused to form liquid-phase contaminator. Portion of obtained liquid-phase contaminator is directed to circulation (6) for dilution of suspension inside said separator while another portion (13) is fed into separator bottom. Liquid phase (14) is discharged from separator bottom while portion of discharged liquid-phase contaminator is removed as the flow of product (16) and another portion is recycled to ejector (17) to be used as the motive fluid.

EFFECT: higher reliability of contaminants removal from separators.

14 cl, 1 dwg

The technical field to which the invention relates

The present invention relates to a method for removal of gaseous pollutants, in particular dioxide of carbon and/or hydrogen sulfide, from the stream of raw gas containing methane and gaseous pollutants. The invention also relates to a device for cryogenic separation to implement the process, and the resulting products.

The level of technology

The removal of acidic pollutants, in particular dioxide of carbon and/or hydrogen sulfide, containing methane gas flows is described in several publications.

In WO 03/062725 describes how to remove frozen particles from the natural gas stream cooling flow of natural gas with the formation of a suspension of solid acidic pollutants in compressed-liquefied natural gas. The solid particles are separated from the liquid with the help of the cyclone. Obviously, the achievement of full separation of liquid and solid particles is a challenge.

In the U.S. patent 4533372 described cryogenic way to remove carbon dioxide and other acid gases from metanosoderzhashchie gas processing raw flow in the zone of distillation and in the regulated nature zone freezing. This method is rather complicated and requires very specific hardware.

In the U.S. patent 3398544 describes how to remove acidic pollutants from the natural gas stream cooling, with the aim of liquefaction flow and partial hardening flow, then there is an extension and Department of purified gas and liquid flows from the solid particles. Solid contaminants must be removed from the separator system, which is a complex process, when it is required to minimize losses of gas liquids.

In WO 2004/070297 describes how to remove pollutants from the natural gas stream. At the first stage of the flow of raw gas water is removed. This is mainly done by cooling flow of raw gas, which leads to the formation of methane hydrates with the subsequent removal of hydrates. Further cooling leads to the formation of solid acidic pollutants. After separation of the solid acidic pollutants receive the flow of purified natural gas. Preferably the transformation of solid pollutants into the liquid is carried out by heating the solid materials.

The problem described in the WO 2004/070297 method is the reliability of removal of pollutants from the separation of the device, as well as remove only pure liquids, not containing solid particles. In this regard, it is noted that a continuous flow of solid particles in the described method can sometimes lead to the formation in the upper part of the heat exchanger of a thick layer of solid material. In addition, a layer of solid material to be deposited and at the bottom of the device, as solid CO 2 has a higher density than the liquid flow. It is important to withdraw from the unit flow net liquid to avoid clogging in the pipe system and/or heat exchangers, as well as damage to pipes and other equipment.

Disclosure of the invention

The aim of the present invention to provide an improved method of cryogenic separation, which would be attractive way possible to overcome the above problems.

Unexpectedly it was revealed that this can be achieved through a certain sequence of the stages of way, using the ejector, the heat exchanger and recycling obtained from the heat exchanger liquid pollutant.

Accordingly, the present invention relates to a method for removal of gaseous contaminants from the stream of raw gas containing methane and gaseous pollutants, which includes:

1) flow of raw gas;

2) cooling flow of the raw gas to the temperature at which a part of the pollutants hardens and forms a suspension, which contains solid pollutant, liquid-phase polluter and enriched with methane gas phase;

3) introduction of suspension obtained at the stage 2)in the upper or middle part of the device cryogenic separation;

4) removal from the top of the device cryogenic separation stream containing enriched with methane gas phase;

5) introduction of stream containing liquid-phase polluter, in the middle and/or lower part of the device cryogenic separation to obtain diluted suspension of contaminants;

6) introduction of diluted suspension pollutants obtained at the stage 5), through the ejector in the heat exchanger in which the solid pollutant present in diluted suspension of contaminants, is melted with the formation of the liquid-phase of the pollutant, and the heat exchanger is located outside separation devices, and the ejector is installed with the outside or inside the device cryogenic separation or partially with internal and partly outside device cryogenic separation;

7) the introduction of part or the entire amount of liquid pollutant obtained at the stage 6), in gas-liquid separator, and gas-liquid separator preferable is the lower part of the unit cryogenic separation;

8) the introduction of part or the entire amount of liquid pollutant obtained at the stage 6), device for separation as described above for stage 5);

9) removal of the gas-liquid separator flow of liquid-phase polluter; and

10) the separation of the flow of liquid pollutant obtained at the stage 9), on the flow of liquid product and recycle stream, which is used in the ejector as the driving (working) the liquid.

The implementation of the invention

According to the present invention obtained continuously moving suspension phase, minimizing the risk of any of zakuporivavshih in the device cryogenic separation or in pipelines and other details of the equipment. In addition, when the heat exchanger is displayed completely liquid flow, the absence of solid pollutant reduces the risk of zakuporivavshih or erosion in the subsequent sections of pipelines or other equipment, thanks to what will not be damaged devices with moving parts, such as pumps. With the purpose of uniform distribution of particulates CO 2 across the heat exchanger preferably use when submitting the materials to the heat exchanger static mixer. In addition, when the heat exchanger is displayed flow net liquid flow is formed relatively cold liquid and, thus, minimizing the need for heat for separation devices, and in the product flow is supported by high volume exchanged cold.

It was observed that described above for stage 7) liquid pollutant, as well as liquid-phase polluter described above for phase 8), can contain some of the steam and/or immediately released gas, for example to 10%mass, it is preferable to 5 wt.%, more preferably to 2 wt.%, in the calculation of the entire quantity of liquid pollutant.

According to the present invention, it is advisable to stream raw gas was the flow of natural gas, in which gaseous pollutants are carbon dioxide, and/or hydrogen sulfide, and/or 2+ -hydrocarbons.

The number of hydrocarbon fractions in the feed gas flow is mainly from 10 to 85 mol. % of the gas flow, preferably from 25 to 80 mol. %. Hydrocarbon fraction from the natural gas stream contains, in particular, at least 75 mol. % methane, preferably 90 mol. %. Hydrocarbon fraction in the flow of natural gas could be acceptable way to be from 0 to 25% vol. 2+ -hydrocarbons, preferably from 0 to 20% 2-6-hydrocarbons, preferably from 0.3 to 18% vol. 2-4-hydrocarbons and especially preferably from 0,5 up to 15% vol. ethane. The gas stream may contain up to 20% and preferably from 0.1 to 10% vol. nitrogen in the calculation of the total gas flow.

With a reasonable amount of carbon dioxide in the gas flow is from 15 to 90%, preferably from 20 to 75%vol and/or acceptable amounts of hydrogen sulphide (in case of its presence in the gas stream) is between 5 and 40%vol preferably from 20 to 35%. These quantities are based on total hydrocarbons, hydrogen sulphide and carbon dioxide. It was noted that this method is especially suitable for gas streams containing large amounts of high-sulphur pollutants, such as 10 or more mol. %, preferably 15 to 90 mol. %.

In method according to the present invention, the flow of raw gas at stage 1) temperature is mainly between -5 up to 150 C, preferably from -10 to 70 C, and a pressure from 10 to 700 bar (abs), preferably from 20 to 200 bar (abs).

The cooling phase 2) of this way it is advisable to use isoenthalpic expansion, preferably using isoenthalpic expansion through the opening or the valve, in particular the valve Joule-Thomson, or cooling is done with the help of close to isentropic expansion, in particular through expander, preferably turboexpander or Laval nozzle. Especially it is preferable valve.

In stage 2) the flow of raw gas is advisable to cool to a temperature from -40 C to -100°C, preferably from -50 C to -80 C.

Before the expansion of the flow of raw gas it is reasonable to cool to a temperature between 15 C up to-45C C, preferably from 5 C to -25 C. In another embodiment, the invention, the flow of raw gas before the extension is pre-cooled to a temperature of 15 to 35°C, preferably from 5 to -20 C.

This preliminary cooling flow of raw gas is reasonable to carry out with the help of heat exchange with cold fluid medium, with external refrigerants such as propane refrigeration cycle, cascade scheme ethane/propane, or a loop with a mixture of refrigerants, or internal technological circuit, preferably flow of carbon dioxide from the stream of hydrogen sulfide or the flow of cold methane.

It is preferable to carry out this way so that almost all the solid pollutant present in diluted suspension of contaminants, melted with the formation of the liquid-phase polluter on stage 6). The expression "nearly all" indicates that melts at least 95% of solid pollutant present in diluted suspensions, in particular, at least 98%. Preferably, when on stage 6) melted all the solid pollutant present in diluted suspension of contaminants.

From 1% to 90% received on stage 6) liquid pollutant, preferably from 5 to 80% vol. received on stage 6) liquid pollutant is entered into the separation device, as described for stage 5). It is also possible to enter into a separation entire volume received on stage 6) liquid pollutant as described for stage 5).

As mentioned, part of the liquid-phase pollutant enter in the Central part of the device division, and the other part of liquid pollutants introduced into the lower part. Mainly from 10 to 100% vol. and preferably from 20 to 95% vol. of the total entered into a separation liquid-phase pollutant injected into the bottom of your device division at the stage 8). The rest of the liquid-phase pollutant mainly introduced in the Central part of the device division.

In the present invention solid pollutant contains mostly carbon dioxide, while liquid-phase polluter usually contains as carbon dioxide and hydrogen sulfide. May be present and small amounts of hydrocarbons.

According to the present invention, the heat exchanger preferably set at a level below installation ejector.

At the stage 10) from 25 to 95% vol. preferably from 30 to 85% vol. flow of liquid-phase polluter derived from devices division at the stage 9), mainly as a driving (working) the fluid in the ejector.

According to the present invention, the jet is used for output of dilute suspension of pollutants from separation devices and direction/the introduction of the mentioned suspension in the heat exchanger. Diluted suspension of contaminants acts as suction fluid in the ejector, while the recycle stream entered in the ejector at the stage 10) acts as the driving (working) liquid.

Ejectors, which is also called the siphons, exhausters, adoctorate or jet pumps, well known and have been described in detail in the existing level of technology. Mentioned here ejector is a device for injection of a suspension of solid and liquid CO 2 from the separator in the heat exchanger. Ejector, primarily meant for use in operations in which the pressure pumping low and below flow pressure motive fluid. For the description of suitable ejectors, also called ejectors or jet pumps, see Perry's Handbook for Chemical engineering, 8 th Edition, chapter 10.2. According to the present invention may be used for any type of ejector. Preferred ejector is Gidrostroy injector bulk phone

Ejector mainly located inside the unit, division or partly within and partly outside separation devices.

It is advisable to place the ejector inside any of the case that allows you to delete the ejector of separation devices. In such a case might be, for example, southtowne protective system, for example, the tube that can be isolated from the process through valves.

In another embodiment of the present invention ejector is located outside separation devices. Such an implementation option can be useful in cases, when used ejector requires repair or replacement.

The jet may be of such size that it is completely entered into a separation or could block all width of separation devices, usually having the form of capacity. However, it can go outside at two points through the inner wall of separation devices.

Stage 7) of this method of liquid-phase polluter is injected into the gas-liquid separator, preferably in the lower part of the device division at a level that is above the level at which the liquid-phase polluter is removed from the bottom of the device division at the stage 9). Liquid-phase polluter may contain some of the steam and/or instantly emitted gas. These couples and/or instantly emitted gas can be removed by means of a separator instantly emitted gas, preferably separator instantly emitted gas, located outside the gas-liquid separator. As a result of introduction of liquid-phase pollutant at a level that is above the level at which liquid is removed polluter, free instantly emitted gas and/or steam can climb towards the top of the device cryogenic separation.

As a rule, enriched with methane gas phase is removed from the top of the device for cryogenic separation at a high level, preferably from the top of the reactor.

Output for enriched with methane gas phase usually has to be above the level at which is received from the heat exchanger, the stream of liquid-phase polluter is entered into a separation stage 5).

The input received at the stage 2) suspension of pollutants should be at a level that is preferably higher than the level at which is received from the heat exchanger, the stream of liquid-phase polluter is entered into a separation stage 5).

Preferably, the level at which the suspension of the polluter is entered into the separation device in stage 3), was above the level in which you will install the heat exchanger.

It should be borne in mind that the ejector is below the level of suspension that is supported in the separation device.

The flow of liquid pollutant removed from the bottom of separation devices, it is advisable to delete below the level of suspension in the separation device.

To prevent the ingress of solid particles on the line output can be used appropriate internal devices. Removal of liquid-phase flow pollutant bottom of the device of division, and to bring into effect the flow of liquid pollutant that will be used as the driving (working) the fluid in the ejector, preferably on line output was installed pump.

Cooling described on the stage (2) of this way, preferably carried out at a short distance from the separation of the device, for example to a few meters, preferably no more than 1 M. Suitable separation device is a tank having a vertical cylindrical body. Diameter can vary from 1 to 10 m or more, the height can vary from 3 up to 35 m or more. As a rule, the level of suspension in the separation device should be from 30 to 70% of the height of the device. The temperature of the suspension mainly in about 1 to 45C preferably from 3 to 40 C higher than the temperature of the polluted gas flow with the introduction of the separation apparatus.

For the heat needed to melt the solid pollutants in the heat exchanger preferably used any process stream. Appropriate technological flow is enriched with methane gas phase.

At stage 5) recirculate liquid pollutant can be entered into a separation and suspension of pollutants to be below the level at which enriched by methane gas phase is deleted from the device division. Thus on the inner walls of the device can be created flush the stream.

In the separation device provides tools for sending diluted suspension of contaminants in the direction of the ejector. For this purpose, mainly using the funnel. One or more of funnels can be placed one above the other. In a broader part of the funnel mainly has a grille that prevents the falling of a large fragments in a more narrow inlet injector/pump and thereby helps to avoid clogging.

Stage 7) liquid-phase polluter mainly introduced in the lower part of the device division at a level that is above the level at which the liquid-phase polluter is removed from the bottom of the device division at the stage 8).

Stage 7) method according to the present invention containing liquid pollutant flow mainly introduced in gas-liquid separator, preferably in the lower part of the device division at a level that is below the level at which the ejector.

The main purpose of introduction to stage 5) of the stream is thinning suspension and depending on the process conditions distillation certain amount of hydrocarbons and/or the preliminary melting certain amount of solid material in suspension of contaminants, which was introduced in the separation device in stage 3).

Stage 8) method according to the present invention containing liquid pollutant flux is removed from the device division at a level that is below the level at which the ejector.

Stage 9) the flow of liquid-phase polluter preferably removed with the help of the pump.

At the stage 10) recycle stream preferably injected directly into the ejector.

The pollutant content-rich methane gas phase removed from the device division at the stage 4), mostly less than 10% vol. and preferably less than 5%.

The flow of raw gas at stage 1) of this method may be subjected to one or more treatment processes, in which gaseous pollutants are removed from the feed gas flow before stage 2) of this method.

Thus, in one of the preferred options for the implementation of the flow of raw gas is obtained through the following stages:

a) flow of untreated raw gas;

b) cooling flow of untreated raw gas to the temperature at which the liquid phase formed the polluter and enriched with methane gas phase; and

c) the separation of the two phases obtained at the stage 2) using gas-liquid separator.

It is advisable two - or three-fold repetition stages a) and (b) before phase 2) according to the present invention. Such way was, for example, described in WO 2006/087332, which is included in this application as a reference material. Therefore, before taking the stage 2) of the present invention, the flow of raw gas can be subjected to several combinations consistently pursued stages cooling and separation.

After the stage of (a) and before the stage 2) according to the present invention preferably, enriched with methane gas phase could be re-compressed at one or more stages of compression.

To achieve methane flow characteristics of pipeline gas and liquefied natural gas obtained at the stage 4) enriched with methane gas phase can be further cleaned using a process cryogenic distillation using section cryogenic distillation, which is known in the existing level of technology.

In this additional process cryogenic distillation preferably, bottom temperature section cryogenic distillation ranged from -30 up to 10 degrees C, preferably from -10 to 5 C. For heat supply in section distillation can be used in the reboiler.

The temperature of the upper section of cryogenic distillation is mainly from -110 -80°C, preferably between -100 -90 C. In the top section of cryogenic distillation can be capacitor to create irrigation and liquefied product (LNG). In the alternative scenario, remaining acidic pollutants can be extracted water aminoven solution, in particular water ethanolamines, such as Diisopropylamine (DIPA), diethanolamine (DEA), etc. Such methods are well known in the existing level of technology.

The present invention refers also to the design of the cryogenic separation for implementing the method according to the present invention, which consists of upper part, middle part and the lower part; means for input of the suspension which contains solid pollutant, liquid-phase polluter and enriched with methane gas phase in the upper or middle part of the device of division; means for removal enriched with methane gas phase from the top of the device of division; the funds for the introduction of stream containing liquid-phase polluter in the upper or middle part of the separation devices for dilution suspension of pollutants inside the device of division; the heat exchanger located outside separation devices; pump for pumping slurry, preferably ejector, located inside or outside the separation devices or partially inside and partially outside separation devices at a level that is below the level at which funds are to enter the suspension of contaminants in the disconnecting device, and the ejector reported with heat exchanger; funds for directions to the ejector diluted suspension of pollutants inside the device of division; means for input received in the heat exchanger liquid pollutant in the gas-liquid separator, preferably in the lower part of the device of division; means for input received in the heat exchanger liquid pollutant in the upper or middle part of the device of division; means for removal of liquid pollutant from the bottom of the device of division; a means to share remote from the bottom of the liquid phase of the pollutant on the flow of liquid product and recycle stream for use as a driving (working) the fluid in the ejector.

Suitable for directions diluted suspension of pollutants within separation devices to the pump for pumping slurry, in particular to the ejector, may include the funnel. It is advisable to use several craters, for example, two-arranged one above the other craters.

Diluted suspension of contaminants may be the preferred way directed from ejector directly into the heat exchanger. However, in another embodiment, before entering diluted suspension of contaminants in the heat exchanger of the latter may be initially skipped across the media type of the pipeline. In this case, the separation device also contains a means of setting diluted suspension of contaminants through the ejector in a heat exchanger.

In that case, when the flow of liquid pollutant contains mainly carbon dioxide and therefore is a CO 2-enriched stream, CO 2-enriched stream is mainly exposed to additional compressed and injected into underground reservoir, primarily for use in enhanced oil recovery or for storage in the aquifer or for storage in an empty oil reservoir. Getting liquid CO 2-enriched stream gives the advantage to pump into underground reservoir of this liquid flow requires less compression equipment. Melted mainly at least 90%, and, preferably, at least 98% of solid acidic pollutants. Thus receive the liquid flow of pollutants, which can easily be transported further.

The present invention also relates to the installation for realization of the above described way.

The present invention also refers to a purified gas flow is obtained by the method according to the present invention.

The present invention also relates to a method for liquefaction flow of raw gas, which includes cleansing flow of raw gas according to the present invention and subsequent liquefaction flow of raw gas using known in the art methods. In that case, when the flow of raw gas is the flow of natural gas, the invention also provides liquefied natural gas (LNG) by cooling obtained by this method purified natural gas.

Further, the invention is illustrated with figure 1. Figure 1 : natural gas flowing through the pipeline 1, passes through the expansion unit 2, in particular the valve Joule-Thomson, resulting in a flow of suspension, which contains solid pollutant, liquid-phase polluter and enriched with methane gas phase. The flow of suspension passes through the pipe 3 in the device 4 cryogenic separation. Enriched with methane gas phase is removed from the separator unit to piping 5. The flow of liquid-phase polluter is entered into the separation device on line 6 to dilute suspension inside the device division, establishing or maintaining a level 7 suspension. Diluted suspension of contaminants is sent through a funnel 8 to the upper hole ejector 9. In the ejector 9 diluted suspension is used as absorbable liquid and through the ejector 9 she comes by pipeline 11 in the heat exchanger 10. In the heat exchanger 10 present in diluted suspension of solid polluter is melted with the formation of the liquid-phase pollutant. Part of the amount thus liquid pollutant is sent through a pipeline 12 to the pipeline 6, while the main part of liquid-phase polluter is introduced in the lower part of the separation unit 4 through pipe 13. Then the liquid-phase polluter is derived from dividing unit 4 through line 14 with a pump 15. Pump 15 may be also situated in the pipeline 17. Part of the extracted liquid pollutant is given as the flow of product through the pipeline 16, and the other part of the specified liquid pollutant recycle pipeline 17 to the ejector 9. There is also a funnel 18 to flow direction suspension towards the crater 18.

1. The way to remove gaseous pollutants from a stream of raw gas containing methane and gaseous pollutants, which includes: 1) flow of raw gas; 2) cooling flow of the raw gas to the temperature at which a part of the pollutants hardens and forms a suspension that contains solid the polluter, liquid-phase polluter and enriched with methane gas phase; 3) introduction obtained at the stage 2) suspension in the upper or middle part of the device cryogenic separation; 4) removal from the top of the device cryogenic separation stream containing enriched with methane gas phase; 5) introduction of stream containing liquid-phase polluter, in the middle or lower part of the device cryogenic separation to obtain diluted suspension of pollutants; 6) obtained at the stage 5) diluted suspension of contaminants through the ejector in a heat exchanger in which solid pollutant present in diluted suspension of contaminants, is melted with the formation of the liquid-phase of the pollutant, and the heat exchanger is located outside separation devices, and the ejector is located inside or outside the unit cryogenic separation or partially inside and partially outside the unit cryogenic separation; 7) introduction part liquid pollutant obtained at the stage 6), in gas-liquid separator, which preferably is the lower part of the unit cryogenic separation; 8) introduction part obtained at the stage 6) liquid pollutant in the device division, as described above on stage 5); 9) removal of liquid-phase flow pollutant from a gas-liquid separator; and 10) the division obtained at the stage of 9) flow of liquid-phase polluter on the flow of liquid product and recycle stream, which is used as the driving fluid in the ejector.

2. The method according to claim 1 in which the flow of raw gas is a natural gas stream, in which gaseous pollutants are carbon dioxide, and/or hydrogen sulfide, and/or 2+ -hydrocarbons.

3. The method of claim 2, in which the flow of natural gas contains 15 to 90%, preferably from 20 to 75% vol. of carbon dioxide.

4. The method of claim 2, or 3, in which the flow of natural gas contains from 0 to 25% vol. C 2+ -hydrocarbons, preferably from 0 to 20% 2-6 of hydrocarbons, preferably from 0.3 and 18% vol. 2-4 of hydrocarbons, preferably from 0 to 20%, especially preferably between 0.5 and 15% vol. ethane and/or in which the flow of natural gas contains from 5 to 40% vol. of hydrogen sulphide, preferably between 20 and 35%.

5. The method of claim 2, or 3, in which the flow of raw gas contains at least 75% vol. methane.

6. The method according to claim 1 or 2, in which the flow of raw gas phase 1) has a temperature from -20 to 150 C, preferably from -10 to 70 C, and a pressure from 10 to 250 bar (abs), preferably from 80 to 120 bar (abs).

7. The method according to claim 1 or 2, in which the cooling stage 2) exercise using isoenthalpic expansion, preferably using isoenthalpic expansion through the opening or the valve, in particular the valve Joule-Thomson, or in which cooling is done with the help of close to isentropic expansion, in particular through expander, preferably turboexpander or Laval nozzle.

8. The method according to claim 7, in which the flow of raw gas before the extension is pre-cooled to a temperature of 15 to 35°C, preferably from 5 to -20 C.

9. The method of claim 8, in which preliminary cooling flow of raw gas is performed by heat exchange with the refrigerant, in particular with external refrigerant, for example, propane cycle, cascade scheme ethane/propane, or cycle with mixtures of refrigerating agents, or internal technological circuit, preferably with a stream of carbon dioxide or the flow of hydrogen sulfide or cold-flow of methane.

10. The method according to claim 1 or 2, in which the flow of raw gas is cooled in stage 2) to a temperature of -40 to -100°C, preferably from -50 -80 C.

11. The method according to claim 1 or 2, in which almost all the solid pollutant present in the suspension of contaminants, melted on stage 6).

12. The method according to claim 1 or 2, which at the stage 7) liquid-phase polluter injected into the bottom of your device division at a level that is above the level at which the liquid phase pollutant removed from the bottom of the device division at the stage 8).

13. The method according to claim 1 or 2, which at the stage 5) stream containing liquid-phase polluter, is injected into the device division at a level that is below the level at which enriched by methane gas phase are removed from the device division at the stage 4).

14. The device cryogenic separation for the implementation of the method according to any one of claims 1 to 13, which consists of upper part, middle part and the lower part; funds for the introduction of suspension containing solid pollutant, liquid-phase polluter and enriched with methane gas phase in the upper or middle part of the device of division; means for removal enriched with methane gas phase from the top of the device of division; the funds for the introduction of stream containing liquid-phase polluter in the upper or middle part of the separation devices to dilute suspension of pollutants inside the device of division; the heat exchanger located outside separation devices; ejector, located inside or outside the separation devices or partially inside and partially outside separation devices at a level that is below the level at which there is a tool for the introduction of suspension of contaminants in the device division, and the ejector reported with heat exchanger; funds for directions to the ejector diluted suspension of pollutants inside the device of division; means for input received in the heat exchanger liquid pollutant in the lower part of the device of division; means for input received in the heat exchanger liquid pollutant in the upper or middle part of the separation devices, each connected by a fluid with specified means for introduction of stream containing liquid-phase polluter in the upper or middle part of the separation devices to dilute suspension of pollutants within separation devices; means for removal of liquid pollutant from the bottom of the device of division; a means to share remote from the bottom of the liquid phase of the pollutant on the flow of liquid product and recycle stream for use as motive fluid in the ejector.