CN104748506A - Device for recycling CO2 from oil field mining assisting tail gas and process thereof - Google Patents
Device for recycling CO2 from oil field mining assisting tail gas and process thereof Download PDFInfo
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- CN104748506A CN104748506A CN201510117712.6A CN201510117712A CN104748506A CN 104748506 A CN104748506 A CN 104748506A CN 201510117712 A CN201510117712 A CN 201510117712A CN 104748506 A CN104748506 A CN 104748506A
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Abstract
The invention belongs to a device for recycling CO2 from oil field mining assisting tail gas and a process thereof. The device comprises a feed gas separating device, a liquid ammonia circulating device and a water circulating device; the feed gas separating device comprises a buffer tank connected with feed gas, the buffer tank is connected with an inlet of a three-stage compressor through a pipe, an outlet of the three-stage compressor is connected with a gas-phase inlet in the upper portion of a first re-boiling device through a tube pass of a first water cooling device, a gas-phase outlet of the first re-boiling device is connected with a gas-phase inlet of a first rectifying tower through a pipe, a mixed gas outlet of the first rectifying tower is connected with the upper portion of a second re-boiling device, a liquid-phase outlet of the second re-boiling device is connected with a tube pass inlet of a first condenser through a pipe, a tube pass outlet of the first condenser is connected with a backflow liquid inlet in the middle of a second rectifying tower through a pipe, and a high-boiling-point material outlet in the bottom of the second rectifying tower is sequentially connected with a tube pass of a subcooler and a liquid CO2 storage tank through pipes. The device has the advantages of being stable in running and being suitable for one well or multiple wells, and suitable for large component fluctuations.
Description
Technical field
The invention belongs to oil field to help and adopt tail gas recycle CO
2technical field, is specifically related to a kind of structure simply, stable, and be applicable to individual well or the use of many wells, the oil field that applicable component fluctuation is larger helps adopts tail gas recycle CO
2device and technique.
Background technology
At present, CO in oil field
2be mainly used in and improve in oil recovery factor project.By CO
2the oil reservoir injecting exhaustion can improve oil recovery factor 7% ~ 25%, while raising recovery ratio, also can extend the oil well production life-span.But, also bring problem on the other hand thus, namely while Oil Generation productive rate increases, be dissolved in the CO in oil
2also along with spilling, surface layer is penetrated out.From the viewpoint of cost and environmental pollution, the CO released in sweep gas
2must reclaim and re-inject in oil reservoir and go, this just requires gas treatment facility CO
2coming with other Component seperation in sweep gas, just needing to reduce investment outlay analyze and research and assess the actual conditions of engineering and various gas handling techniques, to determine a kind of gas disposal being best suited for this project.Oil field sweep gas CO
2treatment facility is usually more complicated than convention acidic gas treating process, and expense is also more expensive, generally comprises compression, dehydration, desulfurization, CO
2and CH
4, C
2h
6and the separation of other heavy hydrocarbon compounds, and can influence each other to separating effect between each component.Therefore, must consider that many factors determines gas disposal according to oil field concrete condition.For CO
2the method be separated is a lot, as absorption method, amines absorption process, ionic liquid absorption cycle, CO
2hydrate separation method, membrane separation process etc.But because oil field sweep gas complicated component, gas flow is large, pressure high is traditional method are difficult to reach requirement.
Summary of the invention
The object of the invention is to overcome defect of the prior art and provide a kind of structure simple, stable, be applicable to individual well or the use of many wells, the oil field that applicable component fluctuation is larger helps adopts tail gas recycle CO
2device and technique.
The object of the present invention is achieved like this: comprise unstripped gas separator, liquefied ammonia EGR and water circle device and form,
A, unstripped gas separator: unstripped gas separator comprises the surge tank be connected with unstripped gas, surge tank is connected with the import of three-stage blower by pipeline, pipeline in three-stage blower between one stage of compression workshop section with two-stage compression workshop section is connected with the tube side of the second water cooler, pipeline between two-stage compression workshop section with three stage compression workshop section is connected with the tube side of the 3rd water cooler, the outlet of three-stage blower is connected with the first reboiler upper gaseous phase import of the first rectifier bottoms by the tube side of the first water cooler, the bottom of the first reboiler is provided with the first reboiler gaseous phase outlet, first reboiler gaseous phase outlet is connected with the gas phase import of the first rectifying column by pipeline, the bottom of the first rectifying column is provided with the first liquid-phase outlet, described first liquid-phase outlet and light crude oil reclaim storage tank and are connected, the top of the first rectifying column is provided with mixed gas outlet, the mixed gas outlet of described first rectifying column is connected with the second reboiler top bottom Second distillation column, the bottom of the second reboiler is provided with the second reboiler liquid-phase outlet, second reboiler liquid-phase outlet is connected with the tube side import of the first condenser by pipeline, the tube side outlet of the first condenser is connected with the phegma import in the middle part of Second distillation column by the phegma import of pipeline respectively at the first rectifying column, high boiling substance outlet bottom Second distillation column by pipeline successively with tube side and the liquid CO of subcooler
2storage tank is connected, the tube side of described subcooler and liquid CO
2pipeline between storage tank is provided with threeway, and first end exports with the tube side of subcooler and is connected, the second end and liquid CO
2the import of storage tank is connected, 3rd end is connected with the tube side import of the second condenser, the tube side outlet of the second condenser is connected with the shell side import of subcooler by pipeline, the shell-side outlet of subcooler and the pipeline between surge tank with three-stage blower are connected, the incoagulable gas outlet at Second distillation column top is connected by the shell side of pipeline with the second condenser, second condenser shell-side outlet is connected with gas-liquid separator by pipeline, liquid-phase outlet bottom gas-liquid separator is connected with the phegma import on Second distillation column top, the gaseous phase outlet at gas-liquid separator top is connected with incoagulable gas recycling can,
B, liquefied ammonia EGR: comprise ammonia storage tank, the outlet of ammonia storage tank is connected by the shell side of pipeline with the first condenser, the shell-side outlet of the first condenser is connected by the shell side of refrigeration unit with the 3rd condenser successively, and the outlet of the shell side of the 3rd condenser is connected with the import of ammonia storage tank;
C, water circle device: comprise cooling tower, the delivery port of cooling tower is connected with water pump, water pump by pipeline respectively with the shell side of three-stage blower cylinder water trapping mouth, the first water cooler, the shell side of the second water cooler, the shell side of the 3rd water cooler is connected with the tube side of the 3rd condenser, the shell-side outlet of the cylinder delivery port of three-stage blower, the shell-side outlet of the first water cooler, the second water cooler, the shell-side outlet of the 3rd water cooler is connected with the water inlet of cooling tower respectively with the tube side outlet of the 3rd condenser.
In described unstripped gas separator, surge tank is connected by the tube side of pipeline with the second water cooler.In described unstripped gas separator, the outlet of three-stage blower is connected with the first reboiler upper gaseous phase import of the first rectifier bottoms by pipeline.Pipeline in described unstripped gas separator Raw air separation between surge tank and the tube side of the second water cooler is provided with the first valve.In described unstripped gas separator, the outlet of three-stage blower and the pipeline of the first reboiler upper gaseous phase import are provided with the second valve.Pipeline in described unstripped gas separator between the outlet of three-stage blower and the tube side of the first water cooler is provided with the 3rd valve, and described first liquid-phase outlet and the light crude oil pipeline reclaimed between storage tank are provided with the 4th valve, described threeway and liquid CO
2pipeline between the import of storage tank is provided with the 5th valve, pipeline between the tube side import of described threeway and the second condenser is provided with the 6th valve, the pipeline that the tube side of the first condenser exports between the phegma import in the middle part of Second distillation column is provided with the 7th valve, pipeline between the phegma import on the liquid-phase outlet bottom gas-liquid separator and Second distillation column top is provided with the 8th valve, and the pipeline between the gaseous phase outlet at gas-liquid separator top and incoagulable gas recycling can 24 is provided with the 9th valve.Pipeline in described liquefied ammonia EGR between the outlet of ammonia storage tank and the shell side of the first condenser is provided with the tenth valve, pipeline between the shell-side outlet of the first condenser and refrigeration unit is provided with the 11 valve, pipeline between the shell side of refrigeration unit and the 3rd condenser is provided with the 12 valve, and the pipeline between the outlet of the shell side of the 3rd condenser and the import of ammonia storage tank is provided with the 13 valve.Pipeline between the delivery port of described water circle device cooling tower and water pump is provided with the 14 valve, water pump respectively with cylinder, the shell side of the first water cooler, the shell side of the second water cooler of three-stage blower, pipeline between the shell side of the 3rd water cooler and the tube side of the 3rd condenser is respectively equipped with the 15 valve, the 16 valve, the 17 valve, the 18 valve and the 19 valve; The shell-side outlet of the cylinder outlet of three-stage blower, the shell-side outlet of the first water cooler, the second water cooler, the shell-side outlet of the 3rd water cooler and the pipeline of the tube side outlet of the 3rd condenser respectively and between the water inlet of cooling tower are respectively equipped with the 20 valve, the 21 valve, the 22 valve, the 23 valve and the 24 valve.
A kind of oil field helps adopts tail gas recycle CO
2technique, this technique for being divided into unstripped gas separation method, liquefied ammonia circulating cooling method and water circulation cooling means:
A, unstripped gas separation method:
Step one: make unstripped gas enter in surge tank 1, the main component of its unstripped gas is: nitrogen, carbon dioxide, methane, ethane, water and light crude oil, and its pressure is 0.5Mpa, and temperature is normal temperature;
Step 2: compression unstripped gas: make the unstripped gas entering surge tank in step one enter the one stage of compression workshop section of three-stage blower successively, the tube side of the second water cooler, two-stage compression workshop section, in the tube side of the 3rd water cooler and three stage compression workshop section, when the outlet of unstripped gas at three-stage blower, its pressure is 5.0Mpa, and temperature is 75 DEG C;
Step 3: separation of lighter crude oil: make the unstripped gas exported by three-stage blower in step 2 enter in the first rectifying column by the tube side of the first water cooler and the first reboiler of the first rectifier bottoms successively, unstripped gas in the first rectifying column through rectifying, high boiling substance is made to enter the first rectifier bottoms, high boiling substance enters light crude oil by the first liquid-phase outlet and reclaims in storage tank, and low-boiling point material enters in the second reboiler by the mixed gas outlet at the first rectifying column top; Described unstripped gas by temperature after the tube side of the first water cooler is: 60 DEG C, described unstripped gas by the temperature after the first reboiler is: 40 DEG C, after described unstripped gas is separated by rectifying in the first rectifying column, the ratio of high boiling substance and low-boiling point material is 23: 77, described light crude oil reclaims in storage tank and comprises light crude oil, carbon dioxide and water, wherein, carbon dioxide to account in surge tank 4% of carbon dioxide in unstripped gas, water to account in surge tank more than 99% of water in unstripped gas, and light crude oil is light crude oil whole in unstripped gas in surge tank; Nitrogen, carbon dioxide is included, methane and ethane in described low-boiling point material;
Step 4: be more than 97% to concentration by reclaiming purifying carbon dioxide: make unstripped gas in step 3 after separation of lighter crude oil successively through the tube side import of the second reboiler liquid-phase outlet, the first condenser, the tube side outlet of the first condenser, then enters in the phegma import in the middle part of the phegma import of the first rectifying column and Second distillation column respectively; The described phegma imported materials gas entering the first rectifying column carries out rectifying through the first rectifying column again, high boiling substance is made to enter the first rectifier bottoms, high boiling substance enters light crude oil by the first liquid-phase outlet and reclaims in storage tank, and low-boiling point material enters in the second reboiler by the mixed gas outlet at the first rectifying column top; Unstripped gas in the described phegma import entered in the middle part of Second distillation column is through Second distillation column rectifying, and the high boiling substance after rectifying enters bottom Second distillation column, and by the tube side that enters subcooler bottom Second distillation column successively and liquid CO
2in storage tank, low-boiling point material enters the shell side of the second condenser by the incoagulable gas outlet at Second distillation column top; Describedly comprise by the high boiling substance after Second distillation column rectifying the carbon dioxide that concentration is more than 97%, surplus is ethane, and its temperature is 0 DEG C; Describedly comprise the carbon dioxide of 50% and the methane of 35% by the low-boiling point material after Second distillation column rectifying, surplus is ethane, is methane whole in unstripped gas described in step one by the methane in the low-boiling point material after Second distillation column rectifying;
Step 5: product is excessively cold: the tube side of subcooler and liquid CO
2pipeline between storage tank is provided with threeway, passed through tube side and the threeway of subcooler by the high boiling substance after Second distillation column rectifying described in above-mentioned steps four, 6th valve, the tube side of the second condenser and the shell side of subcooler enter in the pipeline between surge tank and three-stage blower; After the described tube side by subcooler, the temperature of high boiling substance is-4 DEG C; The described tube side by subcooler and threeway, through the 6th valve throttle to 0.7Mpa, temperature is-49.5 DEG C; After the tube side heat exchange of the second condenser, temperature is increased to-22.9 DEG C, and its temperature after the shell side heat exchange of subcooler is-2 DEG C;
Step 6: separation of methane: to be entered in gas-liquid separator by the shell side of the second condenser by the low-boiling point material after Second distillation column rectifying described in step 4 and carry out gas-liquid separation, gas after gas-liquid separation enters in incoagulable gas recycling can by the gaseous phase outlet at gas-liquid separator top, its liquid enters in Second distillation column by the phegma import on the liquid-phase outlet bottom gas-liquid separator and Second distillation column top, liquid carries out rectifying separation in Second distillation column, high boiling substance after separation enters bottom Second distillation column, and by the tube side that enters subcooler bottom Second distillation column successively and liquid CO
2in storage tank, low-boiling point material enters the shell side of the second condenser by the incoagulable gas outlet at Second distillation column top, repeats to enter in gas-liquid separator and carries out gas-liquid separation, gas after gas-liquid separation consist of 67.6% carbon dioxide, surplus is methane and ethane, gas in described incoagulable gas recycling can is as the source of the gas of pressure-variable adsorption methane device,
B, liquefied ammonia circulating cooling method:
Step one: the liquefied ammonia in ammonia storage tank is depressurized to 0.1MPa by the tenth valve throttle, and temperature is :-33 DEG C, enters in the shell side of the first condenser, carries out heat exchange with the unstripped gas after separation of lighter crude oil in above-mentioned raw materials gas separation method step 4;
Step 2: make the liquefied ammonia in above-mentioned first condenser shell side enter in the shell side of the 3rd condenser by the shell-side outlet of the first condenser and refrigeration unit, and carry out heat exchange with the industry water in the 3rd condenser tube side, liquefied ammonia pressure after heat exchange is: 1.6MPa, and its temperature is: 40 DEG C;
Step 3: make the liquefied ammonia in above-mentioned 3rd condenser shell side by the circumfluence of ammonia storage tank in ammonia storage tank;
C, water circulation cooling means:
Step one: the industry water in cooling tower is forced into: 0.3Mpa ~ 0.4Mpa by water pump, water temperature is: 35 DEG C;
Step 2: make the industry water after pressurization enter cylinder, the shell side of the first water cooler, the shell side of the second water cooler of three-stage blower respectively by pipeline, in the shell side of the 3rd water cooler and the tube side of the 3rd condenser, respectively to cylinder, the shell side of the first water cooler, the shell side of the second water cooler of three-stage blower, the shell side of the 3rd water cooler and the tube side of the 3rd condenser carry out heat exchange cooling, and the cooled water temperature of its heat exchange is: 36 DEG C;
Step 3: make to enter in cooling tower through the cooled industry water of heat exchange respectively by pipeline in step 2, recycle.In described unstripped gas separation method step 2, the unstripped gas of surge tank is made to enter in the tube side of the second water cooler by the first valve; In described unstripped gas separation method step 3, the unstripped gas of three-stage blower outlet is entered in the first reboiler of the first rectifier bottoms by the second valve.
The present invention designs for skid, and have apparatus structure simple, maneuverability, small investment, feature easy and simple to handle, each component of oil field sweep gas all obtains recycling, has really accomplished without discharge, pollution-free, has extraordinary economic and social benefit.The present invention adopts rectification method, not only overcomes traditional gas recovery technology bottleneck, solves the difficult problems such as source of the gas component fluctuation is large, is applicable to individual well or the use of many wells, stable, and greatly reduces the advantage of cost of investment.
Accompanying drawing explanation
Fig. 1 is structural representation of the present invention.
Detailed description of the invention
As shown in Figure 1, the present invention includes unstripped gas separator, liquefied ammonia EGR and water circle device and form,
A, unstripped gas separator: unstripped gas separator comprises the surge tank 1 be connected with unstripped gas, surge tank 1 is connected by the import of pipeline with three-stage blower 2, pipeline in three-stage blower 2 between one stage of compression workshop section with two-stage compression workshop section is connected with the tube side of the second water cooler 30, pipeline between two-stage compression workshop section with three stage compression workshop section is connected with the tube side of the 3rd water cooler 31, the outlet of three-stage blower 2 is connected with the first reboiler 5 upper gaseous phase import bottom the first rectifying column 4 by the tube side of the first water cooler 3, the bottom of the first reboiler 5 is provided with the first reboiler 5 gaseous phase outlet 8, first reboiler 5 gaseous phase outlet 8 is connected by the gas phase import 10 of pipeline with the first rectifying column 4, the bottom of the first rectifying column 4 is provided with the first liquid-phase outlet 6, described first liquid-phase outlet 6 reclaims storage tank 7 with light crude oil and is connected, the top of the first rectifying column 4 is provided with mixed gas outlet 11, the mixed gas outlet 11 of described first rectifying column 4 is connected with the second reboiler 13 top bottom Second distillation column 12, the bottom of the second reboiler 13 is provided with the second reboiler 13 liquid-phase outlet 9, second reboiler 13 liquid-phase outlet 9 is connected by the tube side import of pipeline with the first condenser 15, the tube side outlet of the first condenser 15 is connected with the phegma import 16 in the middle part of Second distillation column 12 by the phegma import 14 of pipeline respectively at the first rectifying column 4, high boiling substance outlet 17 bottom Second distillation column 12 by pipeline successively with tube side and the liquid CO of subcooler 18
2storage tank 19 is connected, the tube side of described subcooler 18 and liquid CO
2pipeline between storage tank 19 is provided with threeway, and first end exports with the tube side of subcooler 18 and is connected, the second end and liquid CO
2the import of storage tank 19 is connected, 3rd end is connected with the tube side import of the second condenser 20, the tube side outlet of the second condenser 20 is connected with the shell side import of subcooler 18 by pipeline, the shell-side outlet of subcooler 18 and the pipeline between surge tank 1 with three-stage blower 2 are connected, the incoagulable gas outlet 21 at Second distillation column 12 top is connected by the shell side of pipeline with the second condenser 20, second condenser 20 shell-side outlet is connected with gas-liquid separator 22 by pipeline, liquid-phase outlet bottom gas-liquid separator 22 is connected with the phegma import 23 on Second distillation column 12 top, the gaseous phase outlet at gas-liquid separator 22 top is connected with incoagulable gas recycling can 24,
B, liquefied ammonia EGR: comprise ammonia storage tank 25, the outlet of ammonia storage tank 25 is connected by the shell side of pipeline with the first condenser 15, the shell-side outlet of the first condenser 15 is connected by the shell side of refrigeration unit 26 with the 3rd condenser 27 successively, and the outlet of the shell side of the 3rd condenser 27 is connected with the import of ammonia storage tank 25;
C, water circle device: comprise cooling tower 28, the delivery port of cooling tower 28 is connected with water pump 29, water pump 29 by pipeline respectively with the shell side of three-stage blower 2 cylinder water trapping mouth, the first water cooler 3, the shell side of the second water cooler 30, the shell side of the 3rd water cooler 31 is connected with the tube side of the 3rd condenser 27, the shell-side outlet of the cylinder delivery port of three-stage blower 2, the shell-side outlet of the first water cooler 3, the second water cooler 30, the shell-side outlet of the 3rd water cooler 31 is connected with the water inlet of cooling tower 28 respectively with the tube side outlet of the 3rd condenser 27.
In described unstripped gas separator, surge tank 1 is connected by the tube side of pipeline with the second water cooler 30.In described unstripped gas separator, the outlet of three-stage blower 2 is connected with the first reboiler 5 upper gaseous phase import bottom the first rectifying column 4 by pipeline.Pipeline in described unstripped gas separator Raw air separation between surge tank 1 and the tube side of the second water cooler 30 is provided with the first valve 32.In described unstripped gas separator, the outlet of three-stage blower 2 and the pipeline of the first reboiler 5 upper gaseous phase import are provided with the second valve 33.Pipeline in described unstripped gas separator between the outlet of three-stage blower 2 and the tube side of the first water cooler 3 is provided with the 3rd valve 34, described first liquid-phase outlet 6 and the light crude oil pipeline reclaimed between storage tank 7 are provided with the 4th valve 35, described threeway and liquid CO
2pipeline between the import of storage tank 19 is provided with the 5th valve 36, pipeline between the tube side import of described threeway and the second condenser 20 is provided with the 6th valve 37, the pipeline that the tube side of the first condenser 15 exports between the phegma import 16 in the middle part of Second distillation column 12 is provided with the 7th valve 38, pipeline between the phegma import 23 on the liquid-phase outlet bottom gas-liquid separator 22 and Second distillation column 12 top is provided with the 8th valve 39, and the pipeline between the gaseous phase outlet at gas-liquid separator 22 top and incoagulable gas recycling can 24 is provided with the 9th valve 40.Pipeline in described liquefied ammonia EGR between the outlet of ammonia storage tank 25 and the shell side of the first condenser 15 is provided with the tenth valve 41, pipeline between the shell-side outlet of the first condenser 15 and refrigeration unit 26 is provided with the 11 valve 42, pipeline between the shell side of refrigeration unit 26 and the 3rd condenser 27 is provided with the 12 valve 43, and the pipeline between the outlet of the shell side of the 3rd condenser 27 and the import of ammonia storage tank 25 is provided with the 13 valve 44.Pipeline between the delivery port of described water circle device cooling tower 28 and water pump 29 is provided with the 14 valve 45, water pump 29 respectively with cylinder, the shell side of the first water cooler 3, the shell side of the second water cooler 30 of three-stage blower 2, pipeline between the shell side of the 3rd water cooler 31 and the tube side of the 3rd condenser 27 is respectively equipped with the 15 valve the 46, the 16 valve the 47, the 17 valve 48, the 18 valve the 49 and the 19 valve 50; The shell-side outlet of the cylinder outlet of three-stage blower 2, the shell-side outlet of the first water cooler 3, the second water cooler 30, the shell-side outlet of the 3rd water cooler 31 and the pipeline of the tube side outlet of the 3rd condenser 27 respectively and between the water inlet of cooling tower 28 are respectively equipped with the 20 valve the 51, the 21 valve the 52, the 22 valve 53, the 23 valve the 54 and the 24 valve 55.
A kind of oil field helps adopts tail gas recycle CO
2technique, this technique for being divided into unstripped gas separation method, liquefied ammonia circulating cooling method and water circulation cooling means:
A, unstripped gas separation method:
Step one: make unstripped gas enter in surge tank 1, the main component of its unstripped gas is: nitrogen, carbon dioxide, methane, ethane, water and light crude oil, and its pressure is 0.5Mpa, and temperature is normal temperature;
Step 2: compression unstripped gas: make the unstripped gas entering surge tank in step one enter the one stage of compression workshop section of three-stage blower 2 successively, the tube side of the second water cooler 30, two-stage compression workshop section, in the tube side of the 3rd water cooler 31 and three stage compression workshop section, when unstripped gas is when the outlet of three-stage blower 2, its pressure is 5.0Mpa, and temperature is 75 DEG C;
Step 3: separation of lighter crude oil: make the unstripped gas that exported by three-stage blower 2 in step 2 enter in the first rectifying column 4 by the first reboiler 5 bottom the tube side of the first water cooler 3 and the first rectifying column 4 successively, unstripped gas in the first rectifying column 4 through rectifying, high boiling substance is made to enter bottom the first rectifying column 4, high boiling substance enters light crude oil by the first liquid-phase outlet 6 and reclaims in storage tank 7, and low-boiling point material enters in the second reboiler 13 by the mixed gas outlet 11 at the first rectifying column 4 top; Described unstripped gas by temperature after the tube side of the first water cooler 3 is: 60 DEG C, described unstripped gas by the temperature after the first reboiler 5 is: 40 DEG C, after described unstripped gas is separated by rectifying in the first rectifying column 4, the ratio of high boiling substance and low-boiling point material is 23: 77, described light crude oil reclaims in storage tank 7 and comprises light crude oil, carbon dioxide and water, wherein, carbon dioxide to account in surge tank 1 4% of carbon dioxide in unstripped gas, water to account in surge tank 1 more than 99% of water in unstripped gas, and light crude oil is light crude oil whole in unstripped gas in surge tank 1; Nitrogen, carbon dioxide is included, methane and ethane in described low-boiling point material;
Step 4: be more than 97% to concentration by reclaiming purifying carbon dioxide: make unstripped gas in step 3 after separation of lighter crude oil successively through the tube side import of the second reboiler 13 liquid-phase outlet 9, first condenser 15, the tube side outlet of the first condenser 15, then enters in the phegma import 16 in the middle part of the phegma import 14 of the first rectifying column 4 and Second distillation column 12 respectively; The described unstripped gas entering the phegma import 14 of the first rectifying column 4 carries out rectifying through the first rectifying column 4 again, high boiling substance is made to enter bottom the first rectifying column 4, high boiling substance enters light crude oil by the first liquid-phase outlet 6 and reclaims in storage tank 7, and low-boiling point material enters in the second reboiler 13 by the mixed gas outlet 11 at the first rectifying column 4 top; Unstripped gas in the described phegma import 16 entered in the middle part of Second distillation column 12 is through Second distillation column 12 rectifying, high boiling substance after rectifying enters bottom Second distillation column 12, and by the tube side that enters subcooler 18 bottom Second distillation column 12 successively and liquid CO
2in storage tank 19, low-boiling point material enters the shell side of the second condenser 20 by the incoagulable gas outlet 21 at Second distillation column 12 top; Describedly comprise by the high boiling substance after Second distillation column 12 rectifying the carbon dioxide that concentration is more than 97%, surplus is ethane, and its temperature is 0 DEG C; Describedly comprise the carbon dioxide of 50% and the methane of 35% by the low-boiling point material after Second distillation column 12 rectifying, surplus is ethane, is methane whole in unstripped gas described in step one by the methane in the low-boiling point material after Second distillation column 12 rectifying;
Step 5: product is excessively cold: the tube side of subcooler 18 and liquid CO
2pipeline between storage tank 19 is provided with threeway, passed through tube side and the threeway of subcooler 18 by the high boiling substance after Second distillation column 12 rectifying described in above-mentioned steps four, the tube side of the 6th valve 37, second condenser 20 and the shell side of subcooler 18 enter in the pipeline between surge tank 1 and three-stage blower 2; After the described tube side by subcooler 18, the temperature of high boiling substance is-4 DEG C; The described tube side by subcooler 18 and threeway, through the 6th valve 37 throttling to 0.7Mpa, temperature is-49.5 DEG C; After the tube side heat exchange of the second condenser 20, temperature is increased to-22.9 DEG C, and its temperature after the shell side heat exchange of subcooler 18 is-2 DEG C;
Step 6: separation of methane: to be entered in gas-liquid separator 22 by the shell side of the second condenser 20 by the low-boiling point material after Second distillation column 12 rectifying described in step 4 and carry out gas-liquid separation, gas after gas-liquid separation enters in incoagulable gas recycling can 24 by the gaseous phase outlet at gas-liquid separator 22 top, its liquid enters in Second distillation column 12 by the phegma import 23 on the liquid-phase outlet bottom gas-liquid separator 22 and Second distillation column 12 top, liquid carries out rectifying separation in Second distillation column 12, high boiling substance after separation enters bottom Second distillation column 12, and by the tube side that enters subcooler 18 bottom Second distillation column 12 successively and liquid CO
2in storage tank 19, low-boiling point material enters the shell side of the second condenser 20 by the incoagulable gas outlet 21 at Second distillation column 12 top, repeats to enter in gas-liquid separator 22 and carries out gas-liquid separation, gas after gas-liquid separation consist of 67.6% carbon dioxide, surplus is methane and ethane, gas in described incoagulable gas recycling can 24 is as the source of the gas of pressure-variable adsorption methane device,
B, liquefied ammonia circulating cooling method:
Step one: the liquefied ammonia in ammonia storage tank 25 is passed through the tenth valve 41 reducing pressure by regulating flow to 0.1MPa, temperature is :-33 DEG C, enters in the shell side of the first condenser 15, carries out heat exchange with the unstripped gas after separation of lighter crude oil in above-mentioned raw materials gas separation method step 4;
Step 2: make the liquefied ammonia in above-mentioned first condenser 15 shell side enter in the shell side of the 3rd condenser 27 by the shell-side outlet of the first condenser 15 and refrigeration unit 26, and carry out heat exchange with the industry water in the 3rd condenser 27 tube side, liquefied ammonia pressure after heat exchange is: 1.6MPa, and its temperature is: 40 DEG C;
Step 3: make the liquefied ammonia in above-mentioned 3rd condenser 27 shell side by the circumfluence of ammonia storage tank 25 in ammonia storage tank 25;
C, water circulation cooling means:
Step one: the industry water in cooling tower 28 is forced into: 0.3Mpa ~ 0.4Mpa by water pump 29, water temperature is: 35 DEG C;
Step 2: make the industry water after pressurization enter cylinder, the shell side of the first water cooler 3, the shell side of the second water cooler 30 of three-stage blower 2 respectively by pipeline, in the shell side of the 3rd water cooler 31 and the tube side of the 3rd condenser 27, respectively to cylinder, the shell side of the first water cooler 3, the shell side of the second water cooler 30 of three-stage blower 2, the shell side of the 3rd water cooler 31 and the tube side of the 3rd condenser 27 carry out heat exchange cooling, and the cooled water temperature of its heat exchange is: 36 DEG C;
Step 3: make to enter in cooling tower 28 respectively by pipeline through the cooled industry water of heat exchange in step 2, recycle.In described unstripped gas separation method step 2, the unstripped gas of surge tank is made to enter in the tube side of the second water cooler 30 by the first valve 32; In described unstripped gas separation method step 3, the unstripped gas that three-stage blower 2 exports is entered in the first reboiler 5 bottom the first rectifying column 4 by the second valve 33.
In order to more detailed explanation the present invention, now the present invention is further elaborated in conjunction with the embodiments.Specific embodiment is as follows:
Embodiment one
A kind of oil field helps adopts tail gas recycle CO
2technique, this technique for being divided into unstripped gas separation method, liquefied ammonia circulating cooling method and water circulation cooling means:
A, unstripped gas separation method:
Step one: make unstripped gas enter in surge tank 1, the main component of its unstripped gas is: nitrogen, carbon dioxide, methane, ethane, water and light crude oil, and its pressure is 0.5Mpa, and temperature is normal temperature;
Step 2: compression unstripped gas: make the unstripped gas entering surge tank in step one enter the one stage of compression workshop section of three-stage blower 2 successively, the tube side of the second water cooler 30, two-stage compression workshop section, in the tube side of the 3rd water cooler 31 and three stage compression workshop section, when unstripped gas is when the outlet of three-stage blower 2, its pressure is 5.0Mpa, and temperature is 75 DEG C;
Step 3: separation of lighter crude oil: make the unstripped gas that exported by three-stage blower 2 in step 2 enter in the first rectifying column 4 by the first reboiler 5 bottom the tube side of the first water cooler 3 and the first rectifying column 4 successively, unstripped gas in the first rectifying column 4 through rectifying, high boiling substance is made to enter bottom the first rectifying column 4, high boiling substance enters light crude oil by the first liquid-phase outlet 6 and reclaims in storage tank 7, and low-boiling point material enters in the second reboiler 13 by the mixed gas outlet 11 at the first rectifying column 4 top; Described unstripped gas by temperature after the tube side of the first water cooler 3 is: 60 DEG C, described unstripped gas by the temperature after the first reboiler 5 is: 40 DEG C, after described unstripped gas is separated by rectifying in the first rectifying column 4, the ratio of high boiling substance and low-boiling point material is 23: 77, described light crude oil reclaims in storage tank 7 and comprises light crude oil, carbon dioxide and water, wherein, carbon dioxide to account in surge tank 1 4% of carbon dioxide in unstripped gas, water to account in surge tank 1 more than 99% of water in unstripped gas, and light crude oil is light crude oil whole in unstripped gas in surge tank 1; Nitrogen, carbon dioxide is included, methane and ethane in described low-boiling point material;
Step 4: be more than 97% to concentration by reclaiming purifying carbon dioxide: make unstripped gas in step 3 after separation of lighter crude oil successively through the tube side import of the second reboiler 13 liquid-phase outlet 9, first condenser 15, the tube side outlet of the first condenser 15, then enters in the phegma import 16 in the middle part of the phegma import 14 of the first rectifying column 4 and Second distillation column 12 respectively; The described unstripped gas entering the phegma import 14 of the first rectifying column 4 carries out rectifying through the first rectifying column 4 again, high boiling substance is made to enter bottom the first rectifying column 4, high boiling substance enters light crude oil by the first liquid-phase outlet 6 and reclaims in storage tank 7, and low-boiling point material enters in the second reboiler 13 by the mixed gas outlet 11 at the first rectifying column 4 top; Unstripped gas in the described phegma import 16 entered in the middle part of Second distillation column 12 is through Second distillation column 12 rectifying, high boiling substance after rectifying enters bottom Second distillation column 12, and by the tube side that enters subcooler 18 bottom Second distillation column 12 successively and liquid CO
2in storage tank 19, low-boiling point material enters the shell side of the second condenser 20 by the incoagulable gas outlet 21 at Second distillation column 12 top; Describedly comprise by the high boiling substance after Second distillation column 12 rectifying the carbon dioxide that concentration is more than 97%, surplus is ethane, and its temperature is 0 DEG C; Describedly comprise the carbon dioxide of 50% and the methane of 35% by the low-boiling point material after Second distillation column 12 rectifying, surplus is ethane, is methane whole in unstripped gas described in step one by the methane in the low-boiling point material after Second distillation column 12 rectifying;
Step 5: product is excessively cold: the tube side of subcooler 18 and liquid CO
2pipeline between storage tank 19 is provided with threeway, passed through tube side and the threeway of subcooler 18 by the high boiling substance after Second distillation column 12 rectifying described in above-mentioned steps four, the tube side of the 6th valve 37, second condenser 20 and the shell side of subcooler 18 enter in the pipeline between surge tank 1 and three-stage blower 2; After the described tube side by subcooler 18, the temperature of high boiling substance is-4 DEG C; The described tube side by subcooler 18 and threeway, through the 6th valve 37 throttling to 0.7Mpa, temperature is-49.5 DEG C; After the tube side heat exchange of the second condenser 20, temperature is increased to-22.9 DEG C, and its temperature after the shell side heat exchange of subcooler 18 is-2 DEG C;
Step 6: separation of methane: to be entered in gas-liquid separator 22 by the shell side of the second condenser 20 by the low-boiling point material after Second distillation column 12 rectifying described in step 4 and carry out gas-liquid separation, gas after gas-liquid separation enters in incoagulable gas recycling can 24 by the gaseous phase outlet at gas-liquid separator 22 top, its liquid enters in Second distillation column 12 by the phegma import 23 on the liquid-phase outlet bottom gas-liquid separator 22 and Second distillation column 12 top, liquid carries out rectifying separation in Second distillation column 12, high boiling substance after separation enters bottom Second distillation column 12, and by the tube side that enters subcooler 18 bottom Second distillation column 12 successively and liquid CO
2in storage tank 19, low-boiling point material enters the shell side of the second condenser 20 by the incoagulable gas outlet 21 at Second distillation column 12 top, repeats to enter in gas-liquid separator 22 and carries out gas-liquid separation, gas after gas-liquid separation consist of 67.6% carbon dioxide, surplus is methane and ethane, gas in described incoagulable gas recycling can 24 is as the source of the gas of pressure-variable adsorption methane device,
B, liquefied ammonia circulating cooling method:
Step one: the liquefied ammonia in ammonia storage tank 25 is passed through the tenth valve 41 reducing pressure by regulating flow to 0.1MPa, temperature is :-33 DEG C, enters in the shell side of the first condenser 15, carries out heat exchange with the unstripped gas after separation of lighter crude oil in above-mentioned raw materials gas separation method step 4;
Step 2: make the liquefied ammonia in above-mentioned first condenser 15 shell side enter in the shell side of the 3rd condenser 27 by the shell-side outlet of the first condenser 15 and refrigeration unit 26, and carry out heat exchange with the industry water in the 3rd condenser 27 tube side, liquefied ammonia pressure after heat exchange is: 1.6MPa, and its temperature is: 40 DEG C;
Step 3: make the liquefied ammonia in above-mentioned 3rd condenser 27 shell side by the circumfluence of ammonia storage tank 25 in ammonia storage tank 25;
C, water circulation cooling means:
Step one: the industry water in cooling tower 28 is forced into: 0.3Mpa ~ 0.4Mpa by water pump 29, water temperature is: 35 DEG C;
Step 2: make the industry water after pressurization enter cylinder, the shell side of the first water cooler 3, the shell side of the second water cooler 30 of three-stage blower 2 respectively by pipeline, in the shell side of the 3rd water cooler 31 and the tube side of the 3rd condenser 27, respectively to cylinder, the shell side of the first water cooler 3, the shell side of the second water cooler 30 of three-stage blower 2, the shell side of the 3rd water cooler 31 and the tube side of the 3rd condenser 27 carry out heat exchange cooling, and the cooled water temperature of its heat exchange is: 36 DEG C;
Step 3: make to enter in cooling tower 28 respectively by pipeline through the cooled industry water of heat exchange in step 2, recycle.In described unstripped gas separation method step 2, the unstripped gas of surge tank is made to enter in the tube side of the second water cooler 30 by the first valve 32; In described unstripped gas separation method step 3, the unstripped gas that three-stage blower 2 exports is entered in the first reboiler 5 bottom the first rectifying column 4 by the second valve 33.
A series of detailed description listed is above only illustrating for feasibility embodiment of the present invention; they are also not used to limit the scope of the invention, all do not depart from the skill of the present invention equivalent implementations done of spirit or change all should be included within protection scope of the present invention.It is to be noted in this article, " first ", " second " etc. only for differentiation each other, but not represent they significance level and order etc.In describing the invention, it will be appreciated that, term " " center ", " longitudinal direction ", " transverse direction ", " on ", D score, " front ", " afterwards ", " left side ", " right side ", " vertically ", " level ", " top ", " end " " interior ", orientation or the position relationship of the instruction such as " outward " are based on orientation shown in the drawings or position relationship, only the present invention for convenience of description and simplified characterization, instead of indicate or imply that the device of indication or element must have specific orientation, with specific azimuth configuration and operation, therefore limitation of the present invention can not be interpreted as.In describing the invention, it should be noted that, unless otherwise clearly defined and limited, term " installation ", " being connected ", " connection " should be interpreted broadly, and such as, can be fixedly connected with, connect integratedly, also can be removably connect; Also can be the connection of two element internals; Can be directly be connected, also indirectly can be connected by intermediary, for the ordinary skill in the art, above-mentioned term concrete meaning in the present invention can be understood as the case may be.
Claims (10)
1. an oil field helps and adopts tail gas recycle CO
2device, comprise unstripped gas separator, liquefied ammonia EGR and water circle device form, it is characterized in that:
A, unstripped gas separator: unstripped gas separator comprises the surge tank (1) be connected with unstripped gas, surge tank (1) is connected by the import of pipeline with three-stage blower (2), pipeline in three-stage blower (2) between one stage of compression workshop section with two-stage compression workshop section is connected with the tube side of the second water cooler (30), pipeline between two-stage compression workshop section with three stage compression workshop section is connected with the tube side of the 3rd water cooler (31), the outlet of three-stage blower (2) is connected with the first reboiler (5) the upper gaseous phase import of the first rectifying column (4) bottom by the tube side of the first water cooler (3), the bottom of the first reboiler (5) is provided with the first reboiler (5) gaseous phase outlet (8), first reboiler (5) gaseous phase outlet (8) is connected with the gas phase import (10) of the first rectifying column (4) by pipeline, the bottom of the first rectifying column (4) is provided with the first liquid-phase outlet (6), described first liquid-phase outlet (6) and light crude oil reclaim storage tank (7) and are connected, the top of the first rectifying column (4) is provided with mixed gas outlet (11), the mixed gas outlet (11) of described first rectifying column (4) is connected with the second reboiler (13) top of Second distillation column (12) bottom, the bottom of the second reboiler (13) is provided with the second reboiler (13) liquid-phase outlet (9), second reboiler (13) liquid-phase outlet (9) is connected by the tube side import of pipeline with the first condenser (15), the tube side outlet of the first condenser (15) is connected with the phegma import (16) at Second distillation column (12) middle part by the phegma import (14) of pipeline respectively at the first rectifying column (4), high boiling substance outlet (17) of Second distillation column (12) bottom by pipeline successively with tube side and the liquid CO of subcooler (18)
2storage tank (19) is connected, the tube side of described subcooler (18) and liquid CO
2pipeline between storage tank (19) is provided with threeway, and first end exports with the tube side of subcooler (18) and is connected, the second end and liquid CO
2the import of storage tank (19) is connected, 3rd end is connected with the tube side import of the second condenser (20), the tube side outlet of the second condenser (20) is connected by the shell side import of pipeline with subcooler (18), the shell-side outlet of subcooler (18) and the pipeline between surge tank (1) with three-stage blower (2) are connected, incoagulable gas outlet (21) at Second distillation column (12) top is connected by the shell side of pipeline with the second condenser (20), second condenser (20) shell-side outlet is connected with gas-liquid separator (22) by pipeline, the liquid-phase outlet of gas-liquid separator (22) bottom is connected with the phegma import (23) on Second distillation column (12) top, the gaseous phase outlet at gas-liquid separator (22) top is connected with incoagulable gas recycling can (24),
B, liquefied ammonia EGR: comprise ammonia storage tank (25), the outlet of ammonia storage tank (25) is connected by the shell side of pipeline with the first condenser (15), the shell-side outlet of the first condenser (15) is connected with the shell side of the 3rd condenser (27) by refrigeration unit (26) successively, and the outlet of the shell side of the 3rd condenser (27) is connected with the import of ammonia storage tank (25);
C, water circle device: comprise cooling tower (28), the delivery port of cooling tower (28) is connected with water pump (29), water pump (29) by pipeline respectively with three-stage blower (2) cylinder water trapping mouth, the shell side of the first water cooler (3), the shell side of the second water cooler (30), the shell side of the 3rd water cooler (31) is connected with the tube side of the 3rd condenser (27), the cylinder delivery port of three-stage blower (2), the shell-side outlet of the first water cooler (3), the shell-side outlet of the second water cooler (30), the shell-side outlet of the 3rd water cooler (31) is connected with the water inlet of cooling tower (28) respectively with the tube side outlet of the 3rd condenser (27).
2. oil field according to claim 1 helps and adopts tail gas recycle CO
2device, it is characterized in that: in described unstripped gas separator, surge tank (1) is connected by the tube side of pipeline with the second water cooler (30).
3. oil field according to claim 1 helps and adopts tail gas recycle CO
2device, it is characterized in that: in described unstripped gas separator, the outlet of three-stage blower (2) is connected by the first reboiler (5) the upper gaseous phase import of pipeline and the first rectifying column (4) bottom.
4. oil field according to claim 2 helps and adopts tail gas recycle CO
2device, it is characterized in that: the pipeline in described unstripped gas separator Raw air separation between surge tank (1) and the tube side of the second water cooler (30) is provided with the first valve (32).
5. oil field according to claim 3 helps and adopts tail gas recycle CO
2device, it is characterized in that: in described unstripped gas separator, the outlet of three-stage blower (2) and the pipeline of the first reboiler (5) upper gaseous phase import are provided with the second valve (33).
6. oil field according to claim 1 helps and adopts tail gas recycle CO
2device, it is characterized in that: the pipeline in described unstripped gas separator between the outlet of three-stage blower (2) and the tube side of the first water cooler (3) is provided with the 3rd valve (34), described first liquid-phase outlet (6) and the light crude oil pipeline reclaimed between storage tank (7) are provided with the 4th valve (35), described threeway and liquid CO
2pipeline between the import of storage tank (19) is provided with the 5th valve (36), pipeline between the tube side import of described threeway and the second condenser (20) is provided with the 6th valve (37), pipeline between the tube side outlet of the first condenser (15) and the phegma import (16) at Second distillation column (12) middle part is provided with the 7th valve (38), pipeline between the liquid-phase outlet of gas-liquid separator (22) bottom and the phegma import (23) on Second distillation column (12) top is provided with the 8th valve (39), pipeline between the gaseous phase outlet at gas-liquid separator (22) top and incoagulable gas recycling can (24) is provided with the 9th valve (40).
7. oil field according to claim 1 helps and adopts tail gas recycle CO
2device, it is characterized in that: the pipeline in described liquefied ammonia EGR between the outlet of ammonia storage tank (25) and the shell side of the first condenser (15) is provided with the tenth valve (41), pipeline between the shell-side outlet of the first condenser (15) and refrigeration unit (26) is provided with the 11 valve (42), pipeline between the shell side of refrigeration unit (26) and the 3rd condenser (27) is provided with the 12 valve (43), pipeline between the outlet of the shell side of the 3rd condenser (27) and the import of ammonia storage tank (25) is provided with the 13 valve (44).
8. oil field according to claim 1 helps and adopts tail gas recycle CO
2device, it is characterized in that: the pipeline between the delivery port of described water circle device cooling tower (28) and water pump (29) is provided with the 14 valve (45), water pump (29) respectively with the cylinder of three-stage blower (2), the shell side of the first water cooler (3), the shell side of the second water cooler (30), pipeline between the shell side of the 3rd water cooler (31) and the tube side of the 3rd condenser (27) is respectively equipped with the 15 valve (46), 16 valve (47), 17 valve (48), 18 valve (49) and the 19 valve (50), the shell-side outlet of the cylinder outlet of three-stage blower (2), the shell-side outlet of the first water cooler (3), the second water cooler (30), the shell-side outlet of the 3rd water cooler (31) and the pipeline of the tube side outlet of the 3rd condenser (27) respectively and between the water inlet of cooling tower (28) are respectively equipped with the 20 valve (51), the 21 valve (52), the 22 valve (53), the 23 valve (54) and the 24 valve (55).
9. an oil field helps and adopts tail gas recycle CO
2technique, it is characterized in that: this technique for being divided into unstripped gas separation method, liquefied ammonia circulating cooling method and water circulation cooling means:
A, unstripped gas separation method:
Step one: make unstripped gas enter in surge tank (1), the main component of its unstripped gas is: nitrogen, carbon dioxide, methane, ethane, water and light crude oil, and its pressure is 0.5Mpa, and temperature is normal temperature;
Step 2: compression unstripped gas: make the unstripped gas entering surge tank in step one enter the one stage of compression workshop section of three-stage blower (2) successively, the tube side of the second water cooler (30), two-stage compression workshop section, in the tube side of the 3rd water cooler (31) and three stage compression workshop section, when unstripped gas is when the outlet of three-stage blower (2), its pressure is 5.0Mpa, and temperature is 75 DEG C;
Step 3: separation of lighter crude oil: make the unstripped gas exported by three-stage blower (2) in step 2 enter in the first rectifying column (4) by the tube side of the first water cooler (3) and first reboiler (5) of the first rectifying column (4) bottom successively, unstripped gas in the first rectifying column (4) through rectifying, high boiling substance is made to enter the first rectifying column (4) bottom, high boiling substance enters light crude oil by the first liquid-phase outlet (6) and reclaims in storage tank (7), low-boiling point material enters in the second reboiler (13) by the mixed gas outlet (11) at the first rectifying column (4) top, described unstripped gas by temperature after the tube side of the first water cooler (3) is: 60 DEG C, described unstripped gas by the temperature after the first reboiler (5) is: 40 DEG C, after described unstripped gas is separated by rectifying in the first rectifying column (4), the ratio of high boiling substance and low-boiling point material is 23: 77, described light crude oil reclaims in storage tank (7) and comprises light crude oil, carbon dioxide and water, wherein, carbon dioxide accounts for 4% of carbon dioxide in surge tank (1) interior unstripped gas, water accounts for more than 99% of water in surge tank (1) interior unstripped gas, light crude oil is light crude oil whole in surge tank (1) interior unstripped gas, nitrogen, carbon dioxide is included, methane and ethane in described low-boiling point material,
Step 4: be more than 97% to concentration by reclaiming purifying carbon dioxide: make unstripped gas in step 3 after separation of lighter crude oil successively through the tube side import of the second reboiler (13) liquid-phase outlet (9), the first condenser (15), the tube side outlet of the first condenser (15), then enters in the phegma import (14) of the first rectifying column (4) and the phegma import (16) at Second distillation column (12) middle part respectively; The described unstripped gas entering the phegma import (14) of the first rectifying column (4) carries out rectifying through the first rectifying column (4) again, high boiling substance is made to enter the first rectifying column (4) bottom, high boiling substance enters light crude oil by the first liquid-phase outlet (6) and reclaims in storage tank (7), and low-boiling point material enters in the second reboiler (13) by the mixed gas outlet (11) at the first rectifying column (4) top; Unstripped gas in the described phegma import (16) entering Second distillation column (12) middle part is through Second distillation column (12) rectifying, high boiling substance after rectifying enters Second distillation column (12) bottom, and enters tube side and the liquid CO of subcooler (18) successively by Second distillation column (12) bottom
2in storage tank (19), low-boiling point material enters the shell side of the second condenser (20) by incoagulable gas outlet (21) at Second distillation column (12) top; Describedly comprise by the high boiling substance after Second distillation column (12) rectifying the carbon dioxide that concentration is more than 97%, surplus is ethane, and its temperature is 0 DEG C; Describedly comprise the carbon dioxide of 50% and the methane of 35% by the low-boiling point material after Second distillation column (12) rectifying, surplus is ethane, is methane whole in unstripped gas described in step one by the methane in the low-boiling point material after Second distillation column (12) rectifying;
Step 5: product is excessively cold: the tube side of subcooler (18) and liquid CO
2pipeline between storage tank (19) is provided with threeway, passed through tube side and the threeway of subcooler (18) by the high boiling substance after Second distillation column (12) rectifying described in above-mentioned steps four, 6th valve (37), the tube side of the second condenser (20) and the shell side of subcooler (18) enter in the pipeline between surge tank (1) and three-stage blower (2); After the described tube side by subcooler (18), the temperature of high boiling substance is-4 DEG C; The described tube side by subcooler (18) and threeway, through the 6th valve (37) throttling to 0.7Mpa, temperature is-49.5 DEG C; After the tube side heat exchange of the second condenser (20), temperature is increased to-22.9 DEG C, and its temperature after the shell side heat exchange of subcooler (18) is-2 DEG C;
Step 6: separation of methane: to be entered in gas-liquid separator (22) by the shell side of the second condenser (20) by the low-boiling point material after Second distillation column (12) rectifying described in step 4 and carry out gas-liquid separation, gas after gas-liquid separation enters in incoagulable gas recycling can (24) by the gaseous phase outlet at gas-liquid separator (22) top, its liquid enters in Second distillation column (12) by the liquid-phase outlet of gas-liquid separator (22) bottom and the phegma import (23) on Second distillation column (12) top, liquid carries out rectifying separation in Second distillation column (12), high boiling substance after separation enters Second distillation column (12) bottom, and tube side and the liquid CO of subcooler (18) is entered successively by Second distillation column (12) bottom
2in storage tank (19), low-boiling point material enters the shell side of the second condenser (20) by incoagulable gas outlet (21) at Second distillation column (12) top, repeats to enter in gas-liquid separator (22) and carries out gas-liquid separation, gas after gas-liquid separation consist of 67.6% carbon dioxide, surplus is methane and ethane, gas in described incoagulable gas recycling can (24) is as the source of the gas of pressure-variable adsorption methane device,
B, liquefied ammonia circulating cooling method:
Step one: the liquefied ammonia in ammonia storage tank (25) is passed through the tenth valve (41) reducing pressure by regulating flow to 0.1MPa, temperature is :-33 DEG C, enter in the shell side of the first condenser (15), carry out heat exchange with the unstripped gas after separation of lighter crude oil in above-mentioned raw materials gas separation method step 4;
Step 2: make the liquefied ammonia in above-mentioned first condenser (15) shell side enter in the shell side of the 3rd condenser (27) by the shell-side outlet of the first condenser (15) and refrigeration unit (26), and carry out heat exchange with the industry water in the 3rd condenser (27) tube side, liquefied ammonia pressure after heat exchange is: 1.6MPa, and its temperature is: 40 DEG C;
Step 3: make the liquefied ammonia in above-mentioned 3rd condenser (27) shell side by the circumfluence of ammonia storage tank (25) in ammonia storage tank (25);
C, water circulation cooling means:
Step one: the industry water in cooling tower (28) is forced into: 0.3Mpa ~ 0.4Mpa by water pump (29), water temperature is: 35 DEG C;
Step 2: make the industry water after pressurization enter cylinder, the shell side of the first water cooler (3), the shell side of the second water cooler (30) of three-stage blower (2) respectively by pipeline, in the shell side of the 3rd water cooler (31) and the tube side of the 3rd condenser (27), respectively to cylinder, the shell side of the first water cooler (3), the shell side of the second water cooler (30) of three-stage blower (2), the shell side of the 3rd water cooler (31) and the tube side of the 3rd condenser (27) carry out heat exchange cooling, and the cooled water temperature of its heat exchange is: 36 DEG C;
Step 3: make to enter in cooling tower (28) respectively by pipeline through the cooled industry water of heat exchange in step 2, recycle.
10. oil field according to claim 9 helps and adopts tail gas recycle CO
2technique, it is characterized in that: in described unstripped gas separation method step 2, make the unstripped gas of surge tank enter in the tube side of the second water cooler (30) by the first valve (32); In described unstripped gas separation method step 3, the unstripped gas that three-stage blower (2) exports is entered in first reboiler (5) of the first rectifying column (4) bottom by the second valve (33).
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| CN201510117712.6A CN104748506B (en) | 2015-03-13 | 2015-03-13 | Device for recycling CO2 from oil field mining assisting tail gas and process thereof |
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| CN114791205A (en) * | 2022-04-22 | 2022-07-26 | 杭州特盈能源技术发展有限公司 | Green electricity efficient conversion low-energy-consumption air separation energy storage and CO 2 Purification and liquefaction process |
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| WO2021016779A1 (en) * | 2019-07-27 | 2021-02-04 | 江西江氨科技有限公司 | Food-grade co2 preparation system |
| CN110440526A (en) * | 2019-07-27 | 2019-11-12 | 江西江氨科技有限公司 | Food-grade carbon-dioxide preparation system |
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