CN104748506B - 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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- CN104748506B CN104748506B CN201510117712.6A CN201510117712A CN104748506B CN 104748506 B CN104748506 B CN 104748506B CN 201510117712 A CN201510117712 A CN 201510117712A CN 104748506 B CN104748506 B CN 104748506B
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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
Helped the invention belongs to oil field and adopt tail gas recycle CO2A kind of technical field, and in particular to simple structure, it is stable,
It is adapted to individual well or many wells is used, the larger oil field of suitable component fluctuation helps adopts tail gas recycle CO2Device and its technique.
Background technology
At present, the CO in oil field2It is mainly used in raising oil recovery factor project.By CO2Injecting can in the oil reservoir of exhaustion
To improve oil recovery factor 7%~25%, while recovery ratio is improved, can also extend the oil well production life-span.But, thus
Bring the problem of another aspect, i.e., it is increased simultaneously in Oil Generation yield, it is dissolved in the CO in oil2Also with spilling, penetrate out
Surface layer.From from the aspect of cost and environmental pollution, the CO released in gas is penetrated2In must reclaiming and re-injecting into oil reservoir
Go, this has required gas treatment facility CO2With penetrate gas in other components separate, it is right to be accomplished by reduce investment outlay
The actual conditions of engineering and various gas handling techniques are analyzed research and assess, to determine a kind of engineering that is best suited for
Gas disposal.Oil field penetrates gas CO2Treatment facility is generally more more complicated than convention acidic gas treating process, and expense is also more high
It is expensive, generally comprise compression, dehydration, desulfurization, CO2And CH4、C2H6And between the separation of other heavy hydrocarbon compounds, and each component
Separating effect can be influenced each other.Therefore, it is necessary to consider many factors according to oil field concrete condition to determine gas treatment side
Case.For CO2The method of separation is a lot, such as absorption method, amines absorption process, ionic liquid absorption cycle, CO2Hydrate
Partition method, membrane separation process etc..But because oil field penetrates the traditional method of the features such as gas complicated component, gas flow are big, pressure is high very
Difficulty reaches requirement.
The content of the invention
A kind of simple structure is provided it is an object of the invention to overcome defect of the prior art, it is stable, it is adapted to
Individual well or many wells are used, and the larger oil field of suitable component fluctuation helps adopts tail gas recycle CO2Device and its technique.
The object of the present invention is achieved like this：Including raw material air separation, liquefied ammonia EGR and water circle device
Constitute,
A, raw material air separation：Raw material air separation includes the surge tank being connected with unstripped gas, and surge tank is by pipe
Road is connected with the import of three-stage blower, the pipeline in three-stage blower between one stage of compression workshop section and two-stage compression workshop section and
The tube side of two water coolers is connected, the tube side phase of pipeline and the 3rd water cooler between two-stage compression workshop section and three stage compression workshop section
Even, the outlet of three-stage blower is entered by the tube side of the first water cooler with the first reboiler upper gaseous phase of first rectifying column bottom
Mouthful it is connected, the bottom of the first reboiler is provided with the first reboiler gaseous phase outlet, the first reboiler gaseous phase outlet is by pipeline and the
The gas phase import of one rectifying column is connected, and the bottom of first rectifying column is provided with the first liquid-phase outlet, first liquid-phase outlet with it is light
Matter crude oil recovery storage tank is connected, and mixed gas outlet, the mixed gas outlet of the first rectifying column are provided with the top of first rectifying column
It is connected with the second reboiler top of Second distillation column bottom, the bottom of the second reboiler is provided with the second reboiler liquid-phase outlet,
Second reboiler liquid-phase outlet is connected by pipeline with the tube side import of the first condenser, and the tube side outlet of the first condenser passes through
Pipeline is connected respectively at the phegma import of first rectifying column with the phegma import in the middle part of Second distillation column, Second distillation column bottom
Portion high boiling substance outlet by pipeline successively with the tube side and liquid CO of subcooler2Storage tank is connected, the pipe of the subcooler
Journey and liquid CO2Pipeline between storage tank is provided with threeway, and first end is connected with the tube side outlet of subcooler, the second end and liquid
CO2The import of storage tank is connected, and the 3rd end is connected with the tube side import of the second condenser, and the tube side outlet of the second condenser is by pipe
Road is connected with the shell side import of subcooler, and the pipeline between the shell-side outlet and surge tank and three-stage blower of subcooler is connected,
Incoagulable gas outlet at the top of Second distillation column is connected by pipeline with the shell side of the second condenser, and the second condenser shell side goes out
Mouthful it is connected with gas-liquid separator by pipeline, the liquid-phase outlet of gas-liquid separator bottom and the phegma on Second distillation column top
Import is connected, and the gaseous phase outlet at the top of gas-liquid separator is connected with incoagulable gas recycling can；
B, liquefied ammonia EGR：Including ammonia storage tank, the outlet of ammonia storage tank is connected by pipeline with the shell side of the first condenser,
The shell-side outlet of the first condenser passes sequentially through refrigeration unit and is connected with the shell side of the 3rd condenser, the shell side of the 3rd condenser
Outlet is connected with the import of ammonia storage tank；
C, water circle device：Including cooling tower, the delivery port of cooling tower is connected with water pump, and water pump is by pipeline respectively with three
Level compresser cylinder water inlet, the shell side of the first water cooler, the shell side of the second water cooler, the shell side of the 3rd water cooler and the 3rd cold
The tube side of condenser is connected, and the cylinder delivery port of three-stage blower, the shell-side outlet of the first water cooler, the shell side of the second water cooler go out
Mouthful, the tube side outlet of the shell-side outlet and the 3rd condenser of the 3rd water cooler is connected with the water inlet of cooling tower respectively.
Surge tank is connected by pipeline with the tube side of the second water cooler in the raw material air separation.The raw material qi leel
The outlet of three-stage blower is connected by pipeline with the first reboiler upper gaseous phase import of first rectifying column bottom in device.
Pipeline in the raw material air separation Central Plains material air separation between the tube side of surge tank and the second water cooler is provided with
First valve.In the raw material air separation on the pipeline of outlet and the first reboiler upper gaseous phase import of three-stage blower
It is provided with the second valve.Pipeline in the raw material air separation between the outlet of three-stage blower and the tube side of the first water cooler
The 3rd valve is provided with, the pipeline that first liquid-phase outlet and light crude oil are reclaimed between storage tank is provided with the 4th valve, institute
State threeway and liquid CO2Pipeline between the import of storage tank is provided with the 5th valve, and the threeway is entered with the tube side of the second condenser
Pipeline between mouthful is provided with the 6th valve, between the phegma import in the middle part of the tube side outlet of the first condenser and Second distillation column
Pipeline be provided with the 7th valve, between the phegma import of the liquid-phase outlet and Second distillation column top of gas-liquid separator bottom
Pipeline is provided with the 8th valve, and the pipeline between gaseous phase outlet and incoagulable gas recycling can 24 at the top of gas-liquid separator is provided with
Nine valves.Pipeline in the liquefied ammonia EGR between the outlet of ammonia storage tank and the shell side of the first condenser is provided with the tenth valve
Door, the pipeline between the shell-side outlet and refrigeration unit of the first condenser is provided with the 11st valve, refrigeration unit and the 3rd condensation
Pipeline between the shell side of device is provided with the 12nd valve, the pipe between the outlet of the shell side of the 3rd condenser and the import of ammonia storage tank
Road is provided with the 13rd valve.Pipeline between the delivery port and water pump of the water circle device cooling tower is provided with the 14th valve,
Water pump cylinder, the shell side of the first water cooler, the shell side of the second water cooler respectively with three-stage blower, the shell side of the 3rd water cooler
And the 3rd condenser tube side between pipeline on be respectively equipped with the 15th valve, the 16th valve, the 17th valve, the 18th
Valve and the 19th valve；The cylinder outlet of three-stage blower, the shell-side outlet of the first water cooler, the shell side of the second water cooler go out
Mouthful, the shell-side outlet of the 3rd water cooler and the tube side of the 3rd condenser are exported on the pipeline respectively and water inlet of cooling tower between
It is respectively equipped with the 20th valve, the 21st valve, the 22nd valve, the 23rd valve and the 24th valve.
A kind of oil field helps adopts tail gas recycle CO2Technique, the technique is to be divided into unstripped gas separation method, liquefied ammonia circulating cooling
Method and water circulation cooling means：
A, unstripped gas separation method：
Step one：Unstripped gas is set to enter in surge tank 1, the main component of its unstripped gas is：Nitrogen, carbon dioxide, methane,
Ethane, water and light crude oil, its pressure are 0.5Mpa, and temperature is normal temperature；
Step 2：Compression unstripped gas：The unstripped gas for entering surge tank in step one is set to sequentially enter the one of three-stage blower
Level compression section, the tube side of the second water cooler, two-stage compression workshop section, in the tube side and three stage compression workshop section of the 3rd water cooler, when
In the outlet of three-stage blower, its pressure is 5.0Mpa to unstripped gas, and temperature is 75 DEG C；
Step 3：Separate light crude oil：The unstripped gas exported by three-stage blower in step 2 is set to pass sequentially through first
The tube side of water cooler and the first reboiler of first rectifying column bottom enter in first rectifying column, and unstripped gas is in first rectifying column
Interior high boiling substance is entered first rectifying column bottom by rectifying, high boiling substance enters lightweight by the first liquid-phase outlet
In crude oil recovery storage tank, low-boiling point material is entered in the second reboiler by the mixed gas outlet at the top of first rectifying column；It is described
Unstripped gas is by temperature after the tube side of the first water cooler：60 DEG C, the unstripped gas is by the temperature after the first reboiler：40
DEG C, the ratio of high boiling substance and low-boiling point material is 23: 77 to the unstripped gas after rectifying is separated in the first rectifying column,
The light crude oil is reclaimed includes light crude oil, carbon dioxide and water in storage tank, wherein, carbon dioxide accounts for unstripped gas in surge tank
The 4% of middle carbon dioxide, water accounts for more than 99% of unstripped gas reclaimed water in surge tank, and light crude oil is complete in unstripped gas in surge tank
The light crude oil in portion；Include nitrogen, carbon dioxide, methane and ethane in the low-boiling point material；
Step 4：It is more than 97% that purifying carbon dioxide to concentration will be reclaimed：After making to separate light crude oil in step 3
Unstripped gas sequentially passes through the tube side import of the second reboiler liquid-phase outlet, the first condenser, and the tube side of the first condenser is exported, so
Respectively enter afterwards first rectifying column phegma import and Second distillation column in the middle part of phegma enter intraoral；It is described to enter the first essence
The phegma imported materials gas for evaporating tower again passes by first rectifying column and carries out rectifying, high boiling substance is entered first rectifying column
Bottom, high boiling substance enters light crude oil and reclaims in storage tank by the first liquid-phase outlet, and low-boiling point material passes through the first rectifying
The mixed gas outlet of top of tower enters in the second reboiler；Phegma in the middle part of the entrance Second distillation column enters intraoral raw material
Gas enters Second distillation column bottom by Second distillation column rectifying, the high boiling substance after rectifying, and by Second distillation column bottom
Portion sequentially enters the tube side and liquid CO of subcooler2In storage tank, low-boiling point material is by the incoagulability gas at the top of Second distillation column
Body outlet enters the shell side of the second condenser；The high boiling substance by after Second distillation column rectifying includes that concentration is 97%
Carbon dioxide above, balance of ethane, its temperature is 0 DEG C；The low-boiling point material bag by after Second distillation column rectifying
Include 50% carbon dioxide and 35% methane, balance of ethane, by the low-boiling point material after Second distillation column rectifying
Methane is methane whole in unstripped gas described in step one；
Step 5：Product is subcooled：The tube side and liquid CO of subcooler2Pipeline between storage tank is provided with threeway, above-mentioned step
Tube side by the high boiling substance after Second distillation column rectifying by subcooler and threeway described in rapid four, the 6th valve, the
In the pipeline that the tube side of two condensers and the shell side of subcooler enter between surge tank and three-stage blower；It is described by subcooler
Tube side after high boiling substance temperature be -4 DEG C；The tube side and threeway by subcooler, through the 6th valve throttle extremely
0.7Mpa, temperature is -49.5 DEG C；- 22.9 DEG C are increased to by temperature after the tube side heat exchange of the second condenser, it is by subcooler
Shell side heat exchange after temperature be -2 DEG C；
Step 6：Separation of methane：Pass through second by the low-boiling point material after Second distillation column rectifying described in step 4
, into gas-liquid separation is carried out in gas-liquid separator, the gas after gas-liquid separation is by the top of gas-liquid separator for the shell side of condenser
Gaseous phase outlet enters in incoagulable gas recycling can, liquid-phase outlet and Second distillation column that its liquid passes through gas-liquid separator bottom
The phegma import on top enters in Second distillation column, and liquid carries out rectifying separation in Second distillation column, the height boiling after separation
Point material enters Second distillation column bottom, and the tube side and liquid CO of subcooler are sequentially entered by Second distillation column bottom2Storage
In tank, low-boiling point material exports the shell side for entering the second condenser by the incoagulable gas at the top of Second distillation column, repeats
Entering carries out gas-liquid separation in gas-liquid separator；The composition of the gas after gas-liquid separation is 67.6% carbon dioxide, balance of first
Alkane and ethane；Gas in the incoagulable gas recycling can as pressure-variable adsorption methane device source of the gas；
B, liquefied ammonia circulating cooling method：
Step one：Liquefied ammonia in ammonia storage tank is depressurized to 0.1MPa by the tenth valve throttle, temperature is：- 33 DEG C, enter
In the shell side of the first condenser, the unstripped gas after light crude oil is separated in method and step four with above-mentioned raw materials qi leel is changed
Heat；
Step 2：Make shell-side outlet and refrigeration unit of the liquefied ammonia in above-mentioned first condenser shell side by the first condenser
Into in the shell side of the 3rd condenser, and exchanged heat with the industry water in the 3rd condenser tube side, the liquefied ammonia pressure after heat exchange
For：1.6MPa, its temperature is：40℃；
Step 3：Make liquefied ammonia in above-mentioned 3rd condenser shell side by the circumfluence of ammonia storage tank to ammonia storage tank；
C, water circulation cooling means：
Step one：The industry water in cooling tower is set to be forced into by water pump：0.3Mpa~0.4Mpa, water temperature is：35℃；
Step 2：Make the industry water after pressurization that the cylinder of three-stage blower, first water cooler are respectively enterd by pipeline
The shell side of shell side, the second water cooler, in the shell side of the 3rd water cooler and the tube side of the 3rd condenser, respectively to three-stage blower
Cylinder, the shell side of the first water cooler, the shell side of the second water cooler, the shell side of the 3rd water cooler and the tube side of the 3rd condenser are carried out
Heat exchange is cooled down, and the water temperature after its heat exchange cooling is：36℃；
Step 3：Make to enter in cooling tower by pipeline respectively by the industry water after the cooling that exchanges heat in step 2, circulation
Use.In the unstripped gas separation method step 2, the unstripped gas of surge tank is set to enter the second water cooler by the first valve
In tube side；In the unstripped gas separation method step 3, the unstripped gas of three-stage blower outlet enters first by the second valve
In first reboiler of rectifier bottoms.
The present invention is designed for skid, simple with apparatus structure, maneuverability, small investment, the characteristics of easy to operate, oil field
The each component for penetrating gas is recycled, and has been truly realized without discharge, pollution-free, with extraordinary economic and society
Benefit.The present invention uses rectification method, not only overcomes traditional gas recovery technology bottleneck, solves the big grade of source of the gas component fluctuation difficult
Topic, is adapted to individual well or many wells are used, stable, and greatly reduces the advantage of cost of investment.
Brief description of the drawings
Fig. 1 is schematic structural view of the invention.
Specific embodiment
As shown in figure 1, the present invention includes that raw material air separation, liquefied ammonia EGR and water circle device are constituted,
A, raw material air separation：Raw material air separation includes the surge tank 1 being connected with unstripped gas, and surge tank 1 passes through
Pipeline is connected with the import of three-stage blower 2, the pipeline in three-stage blower 2 between one stage of compression workshop section and two-stage compression workshop section
Tube side with the second water cooler 30 is connected, the pipeline and the 3rd water cooler 31 between two-stage compression workshop section and three stage compression workshop section
Tube side is connected, and the outlet of three-stage blower 2 is by the tube side of the first water cooler 3 and the first reboiler 5 of the bottom of first rectifying column 4
Upper gaseous phase import is connected, and the bottom of the first reboiler 5 is provided with the gaseous phase outlet 8 of the first reboiler 5, and the gas phase of the first reboiler 5 goes out
Mouth 8 is connected by pipeline with the gas phase import 10 of first rectifying column 4, and the bottom of first rectifying column 4 is provided with the first liquid-phase outlet 6,
First liquid-phase outlet 6 reclaims storage tank 7 and is connected with light crude oil, and the top of first rectifying column 4 is provided with mixed gas outlet 11, institute
State the mixed gas outlet 11 of first rectifying column 4 to be connected with the top of the second reboiler 13 of the bottom of Second distillation column 12, second boils again
The bottom of device 13 is provided with the liquid-phase outlet 9 of the second reboiler 13, and the liquid-phase outlet 9 of the second reboiler 13 passes through pipeline and the first condenser
15 tube side import is connected, and the tube side outlet of the first condenser 15 passes through phegma import of the pipeline respectively at first rectifying column 4
14 are connected with the phegma import 16 at the middle part of Second distillation column 12, and the high boiling substance outlet 17 of the bottom of Second distillation column 12 passes through
Pipeline successively with the tube side and liquid CO of subcooler 182Storage tank 19 is connected, the tube side and liquid CO of the subcooler 182Storage tank 19
Between pipeline be provided with threeway, first end is connected with the tube side outlet of subcooler 18, the second end and liquid CO2Storage tank 19 enters
Mouth is connected, and the 3rd end is connected with the tube side import of the second condenser 20, and the tube side outlet of the second condenser 20 passes through pipeline and mistake
The shell side import of cooler 18 is connected, and the shell-side outlet and the pipeline between surge tank 1 and three-stage blower 2 of subcooler 18 are connected,
The incoagulable gas outlet 21 at the top of Second distillation column 12 is connected by pipeline with the shell side of the second condenser 20, the second condenser
20 shell-side outlets are connected by pipeline with gas-liquid separator 22, liquid-phase outlet and the Second distillation column 12 of the bottom of gas-liquid separator 22
The phegma import 23 on top is connected, and the gaseous phase outlet at the top of gas-liquid separator 22 is connected with incoagulable gas recycling can 24；
B, liquefied ammonia EGR：Including ammonia storage tank 25, the outlet of ammonia storage tank 25 is by pipeline and the shell of the first condenser 15
Cheng Xianglian, the shell-side outlet of the first condenser 15 passes sequentially through refrigeration unit 26 and is connected with the shell side of the 3rd condenser 27, and the 3rd
The outlet of the shell side of condenser 27 is connected with the import of ammonia storage tank 25；
C, water circle device：Including cooling tower 28, the delivery port of cooling tower 28 is connected with water pump 29, and water pump 29 passes through pipeline
Respectively with the cylinder water trapping of three-stage blower 2 mouth, the shell side of the shell side of the first water cooler 3, the second water cooler 30, the 3rd water cooler 31
Shell side and the 3rd condenser 27 tube side be connected, the cylinder delivery port of three-stage blower 2, the shell-side outlet of the first water cooler 3,
The tube side outlet of the shell-side outlet of the second water cooler 30, the shell-side outlet of the 3rd water cooler 31 and the 3rd condenser 27 respectively with it is cool
The water inlet of water tower 28 is connected.
Surge tank 1 is connected by pipeline with the tube side of the second water cooler 30 in the raw material air separation.The raw material
The outlet of three-stage blower 2 is entered by pipeline with the upper gaseous phase of the first reboiler 5 of the bottom of first rectifying column 4 in air separation
Mouth is connected.In the raw material air separation Central Plains material air separation between the tube side of the water cooler 30 of surge tank 1 and second
Pipeline is provided with the first valve 32.The outlet of three-stage blower 2 and the top gas of the first reboiler 5 in the raw material air separation
The pipeline of phase import is provided with the second valve 33.The outlet of three-stage blower 2 and the first water-cooled in the raw material air separation
Pipeline between the tube side of device 3 is provided with the 3rd valve 34, and first liquid-phase outlet 6 and light crude oil are reclaimed between storage tank 7
Pipeline be provided with the 4th valve 35, the threeway and liquid CO2Pipeline between the import of storage tank 19 is provided with the 5th valve 36,
Pipeline between the threeway and the tube side import of the second condenser 20 is provided with the 6th valve 37, and the tube side of the first condenser 15 goes out
Pipeline between the phegma import 16 at mouth and the middle part of Second distillation column 12 is provided with the 7th valve 38, the bottom of gas-liquid separator 22
Pipeline between the phegma import 23 on liquid-phase outlet and the top of Second distillation column 12 is provided with the 8th valve 39, gas-liquid separator 22
Pipeline between the gaseous phase outlet and incoagulable gas recycling can 24 at top is provided with the 9th valve 40.In the liquefied ammonia EGR
Pipeline between the outlet of ammonia storage tank 25 and the shell side of the first condenser 15 is provided with the tenth valve 41, the shell of the first condenser 15
Journey is exported and the pipeline between refrigeration unit 26 is provided with the 11st valve 42, the shell side of the condenser 27 of refrigeration unit 26 and the 3rd it
Between pipeline be provided with the 12nd valve 43, the pipeline between the outlet of the shell side of the 3rd condenser 27 and the import of ammonia storage tank 25 sets
There is the 13rd valve 44.Pipeline between the delivery port and water pump 29 of the water circle device cooling tower 28 is provided with the 14th valve
45, cylinder, the shell side of the first water cooler 3, the shell side of the second water cooler 30, the 3rd water respectively with three-stage blower 2 of water pump 29
The 15th valve 46, the 16th valve are respectively equipped with pipeline between the tube side of the shell side of cooler 31 and the 3rd condenser 27
47th, the 17th valve 48, the 18th valve 49 and the 19th valve 50；The cylinder outlet of three-stage blower 2, the first water cooler 3
Shell-side outlet, the shell-side outlet of the second water cooler 30, the shell-side outlet of the 3rd water cooler 31 and the tube side of the 3rd condenser 27
Outlet is respectively equipped with the 20th valve 51, the 21st valve 52, the with the pipeline between the water inlet of cooling tower 28 respectively
The valve 54 of 22 valve the 53, the 23rd and the 24th valve 55.
A kind of oil field helps adopts tail gas recycle CO2Technique, the technique is to be divided into unstripped gas separation method, liquefied ammonia circulating cooling
Method and water circulation cooling means：
A, unstripped gas separation method：
Step one：Unstripped gas is set to enter in surge tank 1, the main component of its unstripped gas is：Nitrogen, carbon dioxide, methane,
Ethane, water and light crude oil, its pressure are 0.5Mpa, and temperature is normal temperature；
Step 2：Compression unstripped gas：The unstripped gas for entering surge tank in step one is set to sequentially enter the one of three-stage blower 2
Level compression section, the tube side of the second water cooler 30, two-stage compression workshop section, the tube side of the 3rd water cooler 31 and three stage compression workshop section
Interior, when outlet of the unstripped gas in three-stage blower 2, its pressure is 5.0Mpa, and temperature is 75 DEG C；
Step 3：Separate light crude oil：The unstripped gas exported by three-stage blower 2 in step 2 is set to pass sequentially through first
The tube side of water cooler 3 and first reboiler 5 of the bottom of first rectifying column 4 enter in first rectifying column 4, and unstripped gas is in the first rectifying
By rectifying in tower 4, high boiling substance is set to enter the bottom of first rectifying column 4, high boiling substance is entered by the first liquid-phase outlet 6
Light crude oil is reclaimed in storage tank 7, and low-boiling point material enters the second reboiler by the mixed gas outlet 11 at the top of first rectifying column 4
In 13；The unstripped gas is by temperature after the tube side of the first water cooler 3：60 DEG C, the unstripped gas is by after the first reboiler 5
Temperature be：40 DEG C, the unstripped gas is in first rectifying column 4 by high boiling substance after rectifying separation and low-boiling point material
Ratio is 23: 77, and the light crude oil is reclaimed includes light crude oil, carbon dioxide and water in storage tank 7, wherein, carbon dioxide is accounted for
In surge tank 1 in unstripped gas carbon dioxide 4%, water accounts for more than 99% of unstripped gas reclaimed water in surge tank 1, and light crude oil is slow
Rush light crude oils whole in unstripped gas in tank 1；Include nitrogen, carbon dioxide, methane and ethane in the low-boiling point material；
Step 4：It is more than 97% that purifying carbon dioxide to concentration will be reclaimed：After making to separate light crude oil in step 3
Unstripped gas sequentially passes through the liquid-phase outlet 9 of the second reboiler 13, the tube side import of the first condenser 15, the tube side of the first condenser 15
Outlet, then respectively enters in the phegma import 14 of first rectifying column 4 and the phegma import 16 at the middle part of Second distillation column 12；
The unstripped gas of the phegma import 14 of the entrance first rectifying column 4 again passes by first rectifying column 4 and carries out rectifying, makes higher boiling
Material enters the bottom of first rectifying column 4, and high boiling substance enters light crude oil and reclaims in storage tank 7 by the first liquid-phase outlet 6, low
Boilers are entered in the second reboiler 13 by the mixed gas outlet 11 at the top of first rectifying column 4；It is described to enter the second rectifying
By the rectifying of Second distillation column 12, the high boiling substance after rectifying enters the to unstripped gas in the phegma import 16 at the middle part of tower 12
The bottom of two rectifying column 12, and the tube side and liquid CO of subcooler 18 are sequentially entered by the bottom of Second distillation column 122In storage tank 19,
Low-boiling point material exports 21 shell sides for entering the second condenser 20 by the incoagulable gas at the top of Second distillation column 12；It is described logical
The high boiling substance crossed after the rectifying of Second distillation column 12 includes the carbon dioxide that concentration is more than 97%, balance of ethane, its temperature
Spend is 0 DEG C；The low-boiling point material by after the rectifying of Second distillation column 12 includes 50% carbon dioxide and 35% first
Alkane, balance of ethane, by the methane in the low-boiling point material after the rectifying of Second distillation column 12 be step one described in unstripped gas
Middle whole methane；
Step 5：Product is subcooled：The tube side and liquid CO of subcooler 182Pipeline between storage tank 19 is provided with threeway, on
State the tube side described in step 4 by the high boiling substance after the rectifying of Second distillation column 12 by subcooler 18 and threeway, the 6th
The pipeline that valve 37, the tube side of the second condenser 20 and the shell side of subcooler 18 enter between surge tank 1 and three-stage blower 2
It is interior；The temperature by high boiling substance after the tube side of subcooler 18 is -4 DEG C；It is described by the tube side of subcooler 18 and three
It is logical, throttled to 0.7Mpa through the 6th valve 37, temperature is -49.5 DEG C；By temperature liter after the tube side heat exchange of the second condenser 20
Up to -22.9 DEG C, it is -2 DEG C by temperature after the shell side heat exchange of subcooler 18；
Step 6：Separation of methane：By the low-boiling point material after the rectifying of Second distillation column 12 by the described in step 4
The shell side of two condensers 20 carries out gas-liquid separation into gas-liquid separator 22 is interior, and the gas after gas-liquid separation passes through gas-liquid separator
The gaseous phase outlet at 22 tops enters in incoagulable gas recycling can 24, the liquid-phase outlet that its liquid passes through the bottom of gas-liquid separator 22
Phegma import 23 with the top of Second distillation column 12 enters in Second distillation column 12, and liquid carries out essence in Second distillation column 12
Cut is from the high boiling substance after separation enters the bottom of Second distillation column 12, and is sequentially entered by the bottom of Second distillation column 12
The tube side and liquid CO of subcooler 182In storage tank 19, low-boiling point material is gone out by the incoagulable gas at the top of Second distillation column 12
Mouth 21 enters the shell side of the second condenser 20, repeats to carry out gas-liquid separation into gas-liquid separator 22；Gas after gas-liquid separation
The composition of body is 67.6% carbon dioxide, balance of methane and ethane；Gas in the incoagulable gas recycling can 24 is made
It is the source of the gas of pressure-variable adsorption methane device；
B, liquefied ammonia circulating cooling method：
Step one：By the liquefied ammonia in ammonia storage tank 25 by the reducing pressure by regulating flow of the tenth valve 41 to 0.1MPa, temperature is：-33
DEG C, into the shell side of the first condenser 15, the raw material after light crude oil is separated in method and step four with above-mentioned raw materials qi leel
Gas is exchanged heat；
Step 2：Make shell-side outlet and refrigeration of the liquefied ammonia in the above-mentioned shell side of first condenser 15 by the first condenser 15
Unit 26 enters in the shell side of the 3rd condenser 27, and is exchanged heat with the industry water in the tube side of the 3rd condenser 27, after heat exchange
Liquefied ammonia pressure be：1.6MPa, its temperature is：40℃；
Step 3：Make liquefied ammonia in the above-mentioned shell side of 3rd condenser 27 by the circumfluence of ammonia storage tank 25 to ammonia storage tank 25
It is interior；
C, water circulation cooling means：
Step one：The industry water in cooling tower 28 is set to be forced into by water pump 29：0.3Mpa~0.4Mpa, water temperature is：35
℃；
Step 2：Make the industry water after pressurization that the cylinder of three-stage blower 2, the first water cooler 3 are respectively enterd by pipeline
Shell side, the shell side of the second water cooler 30, in the shell side of the 3rd water cooler 31 and the tube side of the 3rd condenser 27, respectively to three-level
The cylinder of compressor 2, 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 and the 3rd cold
The tube side of condenser 27 carries out heat exchange cooling, and the water temperature after its heat exchange cooling is：36℃；
Step 3：Make to enter in cooling tower 28 by pipeline respectively by the industry water after the cooling that exchanges heat in step 2, follow
Ring is used.In the unstripped gas separation method step 2, the unstripped gas of surge tank is set to enter the second water-cooled by the first valve 32
In the tube side of device 30；In the unstripped gas separation method step 3, the unstripped gas of the outlet of three-stage blower 2 passes through the second valve 33
Into in the first reboiler 5 of the bottom of first rectifying column 4.
For the more detailed explanation present invention, the present invention is further elaborated in conjunction with embodiment.Specific embodiment
It is as follows：
Embodiment one
A kind of oil field helps adopts tail gas recycle CO2Technique, the technique is to be divided into unstripped gas separation method, liquefied ammonia circulating cooling
Method and water circulation cooling means：
A, unstripped gas separation method：
Step one：Unstripped gas is set to enter in surge tank 1, the main component of its unstripped gas is：Nitrogen, carbon dioxide, methane,
Ethane, water and light crude oil, its pressure are 0.5Mpa, and temperature is normal temperature；
Step 2：Compression unstripped gas：The unstripped gas for entering surge tank in step one is set to sequentially enter the one of three-stage blower 2
Level compression section, the tube side of the second water cooler 30, two-stage compression workshop section, the tube side of the 3rd water cooler 31 and three stage compression workshop section
Interior, when outlet of the unstripped gas in three-stage blower 2, its pressure is 5.0Mpa, and temperature is 75 DEG C；
Step 3：Separate light crude oil：The unstripped gas exported by three-stage blower 2 in step 2 is set to pass sequentially through first
The tube side of water cooler 3 and first reboiler 5 of the bottom of first rectifying column 4 enter in first rectifying column 4, and unstripped gas is in the first rectifying
By rectifying in tower 4, high boiling substance is set to enter the bottom of first rectifying column 4, high boiling substance is entered by the first liquid-phase outlet 6
Light crude oil is reclaimed in storage tank 7, and low-boiling point material enters the second reboiler by the mixed gas outlet 11 at the top of first rectifying column 4
In 13；The unstripped gas is by temperature after the tube side of the first water cooler 3：60 DEG C, the unstripped gas is by after the first reboiler 5
Temperature be：40 DEG C, the unstripped gas is in first rectifying column 4 by high boiling substance after rectifying separation and low-boiling point material
Ratio is 23: 77, and the light crude oil is reclaimed includes light crude oil, carbon dioxide and water in storage tank 7, wherein, carbon dioxide is accounted for
In surge tank 1 in unstripped gas carbon dioxide 4%, water accounts for more than 99% of unstripped gas reclaimed water in surge tank 1, and light crude oil is slow
Rush light crude oils whole in unstripped gas in tank 1；Include nitrogen, carbon dioxide, methane and ethane in the low-boiling point material；
Step 4：It is more than 97% that purifying carbon dioxide to concentration will be reclaimed：After making to separate light crude oil in step 3
Unstripped gas sequentially passes through the liquid-phase outlet 9 of the second reboiler 13, the tube side import of the first condenser 15, the tube side of the first condenser 15
Outlet, then respectively enters in the phegma import 14 of first rectifying column 4 and the phegma import 16 at the middle part of Second distillation column 12；
The unstripped gas of the phegma import 14 of the entrance first rectifying column 4 again passes by first rectifying column 4 and carries out rectifying, makes higher boiling
Material enters the bottom of first rectifying column 4, and high boiling substance enters light crude oil and reclaims in storage tank 7 by the first liquid-phase outlet 6, low
Boilers are entered in the second reboiler 13 by the mixed gas outlet 11 at the top of first rectifying column 4；It is described to enter the second rectifying
By the rectifying of Second distillation column 12, the high boiling substance after rectifying enters the to unstripped gas in the phegma import 16 at the middle part of tower 12
The bottom of two rectifying column 12, and the tube side and liquid CO of subcooler 18 are sequentially entered by the bottom of Second distillation column 122In storage tank 19,
Low-boiling point material exports 21 shell sides for entering the second condenser 20 by the incoagulable gas at the top of Second distillation column 12；It is described logical
The high boiling substance crossed after the rectifying of Second distillation column 12 includes the carbon dioxide that concentration is more than 97%, balance of ethane, its temperature
Spend is 0 DEG C；The low-boiling point material by after the rectifying of Second distillation column 12 includes 50% carbon dioxide and 35% methane,
Balance of ethane is complete in the methane in the low-boiling point material after the rectifying of Second distillation column 12 is for unstripped gas described in step one
The methane in portion；
Step 5：Product is subcooled：The tube side and liquid CO of subcooler 182Pipeline between storage tank 19 is provided with threeway, on
State the tube side described in step 4 by the high boiling substance after the rectifying of Second distillation column 12 by subcooler 18 and threeway, the 6th
The pipeline that valve 37, the tube side of the second condenser 20 and the shell side of subcooler 18 enter between surge tank 1 and three-stage blower 2
It is interior；The temperature by high boiling substance after the tube side of subcooler 18 is -4 DEG C；It is described by the tube side of subcooler 18 and three
It is logical, throttled to 0.7Mpa through the 6th valve 37, temperature is -49.5 DEG C；By temperature liter after the tube side heat exchange of the second condenser 20
Up to -22.9 DEG C, it is -2 DEG C by temperature after the shell side heat exchange of subcooler 18；
Step 6：Separation of methane：By the low-boiling point material after the rectifying of Second distillation column 12 by the described in step 4
The shell side of two condensers 20 carries out gas-liquid separation into gas-liquid separator 22 is interior, and the gas after gas-liquid separation passes through gas-liquid separator
The gaseous phase outlet at 22 tops enters in incoagulable gas recycling can 24, the liquid-phase outlet that its liquid passes through the bottom of gas-liquid separator 22
Phegma import 23 with the top of Second distillation column 12 enters in Second distillation column 12, and liquid carries out essence in Second distillation column 12
Cut is from the high boiling substance after separation enters the bottom of Second distillation column 12, and is sequentially entered by the bottom of Second distillation column 12
The tube side and liquid CO of subcooler 182In storage tank 19, low-boiling point material is gone out by the incoagulable gas at the top of Second distillation column 12
Mouth 21 enters the shell side of the second condenser 20, repeats to carry out gas-liquid separation into gas-liquid separator 22；Gas after gas-liquid separation
The composition of body is 67.6% carbon dioxide, balance of methane and ethane；Gas in the incoagulable gas recycling can 24 is made
It is the source of the gas of pressure-variable adsorption methane device；
B, liquefied ammonia circulating cooling method：
Step one：By the liquefied ammonia in ammonia storage tank 25 by the reducing pressure by regulating flow of the tenth valve 41 to 0.1MPa, temperature is：- 33 DEG C,
Into in the shell side of the first condenser 15, the unstripped gas after light crude oil is separated in method and step four with above-mentioned raw materials qi leel enters
Row heat exchange；
Step 2：Make shell-side outlet and refrigeration of the liquefied ammonia in the above-mentioned shell side of first condenser 15 by the first condenser 15
Unit 26 enters in the shell side of the 3rd condenser 27, and is exchanged heat with the industry water in the tube side of the 3rd condenser 27, after heat exchange
Liquefied ammonia pressure be：1.6MPa, its temperature is：40℃；
Step 3：Make liquefied ammonia in the above-mentioned shell side of 3rd condenser 27 by the circumfluence of ammonia storage tank 25 to ammonia storage tank 25
It is interior；
C, water circulation cooling means：
Step one：The industry water in cooling tower 28 is set to be forced into by water pump 29：0.3Mpa~0.4Mpa, water temperature is：35
℃；
Step 2：Make the industry water after pressurization that the cylinder of three-stage blower 2, the first water cooler 3 are respectively enterd by pipeline
Shell side, the shell side of the second water cooler 30, in the shell side of the 3rd water cooler 31 and the tube side of the 3rd condenser 27, respectively to three-level
The cylinder of compressor 2, 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 and the 3rd cold
The tube side of condenser 27 carries out heat exchange cooling, and the water temperature after its heat exchange cooling is：36℃；
Step 3：Make to enter in cooling tower 28 by pipeline respectively by the industry water after the cooling that exchanges heat in step 2, follow
Ring is used.In the unstripped gas separation method step 2, the unstripped gas of surge tank is set to enter the second water-cooled by the first valve 32
In the tube side of device 30；In the unstripped gas separation method step 3, the unstripped gas of the outlet of three-stage blower 2 passes through the second valve 33
Into in the first reboiler 5 of the bottom of first rectifying column 4.
Those listed above is a series of to be described in detail only for feasibility implementation method of the invention specifically
Bright, they simultaneously are not used to limit the scope of the invention, all equivalent implementations made without departing from skill spirit of the present invention
Or change should be included within the scope of the present invention.It is to be noted that herein, " first ", " second " etc. are only used
In mutual differentiation, rather than represent their significance level and order etc..In the description of the invention, it is to be understood that art
Language " " center ", " longitudinal direction ", " transverse direction ", " on ", D score, "front", "rear", "left", "right", " vertical ", " level ", " top ", " bottom "
The orientation or position relationship of the instructions such as " interior ", " outward " are, based on orientation shown in the drawings or position relationship, to be for only for ease of and retouch
The present invention is stated to be described with simplified, must be with specific orientation, with specific rather than the device or element for indicating or imply meaning
Azimuth configuration and operation, therefore be not considered as limiting the invention.In the description of the invention, it is necessary to illustrate,
Unless otherwise clearly defined and limited, term " installation ", " connected ", " connection " should be interpreted broadly, for example, it may be fixed
Connection, is integrally connected, or is detachably connected；Can also be two connections of element internal；Can be joined directly together,
Can also be indirectly connected to by intermediary, for the ordinary skill in the art, can understood as the case may be
Above-mentioned term concrete meaning in the present invention.
Claims (10)
1. a kind of oil field helps and adopts tail gas recycle CO2Device, including raw material air separation, liquefied ammonia EGR and water circulation dress
Put, it is characterised in that：
A, raw material air separation：Raw material air separation includes the surge tank (1) being connected with unstripped gas, and surge tank (1) passes through
Pipeline is connected with the import of three-stage blower (2), in three-stage blower (2) between one stage of compression workshop section and two-stage compression workshop section
Pipeline is connected with the tube side of the second water cooler (30), pipeline and the 3rd water-cooled between two-stage compression workshop section and three stage compression workshop section
The tube side of device (31) is connected, and the outlet of three-stage blower (2) passes through tube side and first rectifying column (4) bottom of the first water cooler (3)
First reboiler (5) upper gaseous phase import in portion is connected, and the bottom of the first reboiler (5) is provided with the first reboiler (5) gas phase and goes out
Mouth (8), the first reboiler (5) gaseous phase outlet (8) are connected by pipeline with the gas phase import (10) of first rectifying column (4), and first
The bottom of rectifying column (4) is provided with the first liquid-phase outlet (6), and first liquid-phase outlet (6) reclaims storage tank (7) phase with light crude oil
Even, be provided with mixed gas outlet (11) at the top of first rectifying column (4), the mixed gas outlet (11) of the first rectifying column (4) with
Second reboiler (13) top of Second distillation column (12) bottom is connected, and the bottom of the second reboiler (13) is provided with the second reboiler
(13) liquid-phase outlet (9), the tube side import phase that the second reboiler (13) liquid-phase outlet (9) pass through pipeline and the first condenser (15)
Even, the outlet of the tube side of the first condenser (15) by pipeline respectively with the phegma import (14) of first rectifying column (4) and second
Phegma import (16) in the middle part of rectifying column (12) is connected, and high boiling substance outlet (17) of Second distillation column (12) bottom passes through
Pipeline successively with the tube side and liquid CO of subcooler (18)2Storage tank (19) is connected, the tube side and liquid CO of the subcooler (18)2
Pipeline between storage tank (19) is provided with threeway, and first end is connected with the tube side outlet of subcooler (18), the second end and liquid CO2
The import of storage tank (19) is connected, and the 3rd end is connected with the tube side import of the second condenser (20), the tube side of the second condenser (20)
Outlet is connected by pipeline with the shell side import of subcooler (18), the shell-side outlet and surge tank (1) and three-level of subcooler (18)
Pipeline between compressor (2) is connected, and incoagulable gas outlet (21) at the top of Second distillation column (12) is by pipeline and second
The shell side of condenser (20) is connected, and the second condenser (20) shell-side outlet is connected by pipeline with gas-liquid separator (22), gas-liquid
The liquid-phase outlet of separator (22) bottom is connected with the phegma import (23) on Second distillation column (12) top, gas-liquid separator
(22) gaseous phase outlet at the top of is connected with incoagulable gas recycling can (24)；
B, liquefied ammonia EGR：Including ammonia storage tank (25), the outlet of ammonia storage tank (25) is by pipeline and the first condenser (15)
Shell side is connected, and the shell-side outlet of the first condenser (15) passes sequentially through the shell side phase of refrigeration unit (26) and the 3rd condenser (27)
Even, 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：Including cooling tower (28), the delivery port of cooling tower (28) is connected with water pump (29), and water pump (29) passes through
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 tube side of the shell side of three water coolers (31) and the 3rd condenser (27) is connected, the cylinder delivery port of three-stage blower (2), the first water
The shell-side outlet of cooler (3), the shell-side outlet of the second water cooler (30), the shell-side outlet of the 3rd water cooler (31) and the 3rd are condensed
The water inlet that the tube side of device (27) exports respectively with cooling tower (28) is connected.
2. oil field according to claim 1 helps and adopts tail gas recycle CO2Device, it is characterised in that：The unstripped gas separates dress
Middle surge tank (1) is put to be connected with the tube side of the second water cooler (30) by pipeline.
3. oil field according to claim 1 helps and adopts tail gas recycle CO2Device, it is characterised in that：The unstripped gas separates dress
The outlet of middle three-stage blower (2) is put by the first reboiler (5) upper gaseous phase import of pipeline and first rectifying column (4) bottom
It is connected.
4. oil field according to claim 2 helps and adopts tail gas recycle CO2Device, it is characterised in that：The unstripped gas separates dress
The pipeline put between the tube side of surge tank (1) and the second water cooler (30) in raw material air separation is provided with the first valve
(32)。
5. oil field according to claim 3 helps and adopts tail gas recycle CO2Device, it is characterised in that：The unstripped gas separates dress
The pipeline for putting outlet Yu the first reboiler (5) upper gaseous phase import of three-stage blower (2) is provided with the second valve (33).
6. oil field according to claim 1 helps and adopts tail gas recycle CO2Device, it is characterised in that：The unstripped gas separates dress
Put the pipeline between the outlet of three-stage blower (2) and the tube side of the first water cooler (3) and be provided with the 3rd valve (34), it is described
The pipeline that first liquid-phase outlet (6) and light crude oil are reclaimed between storage tank (7) is provided with the 4th valve (35), the threeway and liquid
Body CO2Pipeline between the import of storage tank (19) is provided with the tube side of the 5th valve (36), the threeway and the second condenser (20)
Pipeline between import is provided with the 6th valve (37), in the middle part of the tube side outlet of the first condenser (15) and Second distillation column (12)
Pipeline between phegma import (16) is provided with the 7th valve (38), the liquid-phase outlet of gas-liquid separator (22) bottom and the second essence
Evaporate the pipeline between the phegma import (23) on tower (12) top and be provided with the 8th valve (39), the gas at the top of gas-liquid separator (22)
Mutually the pipeline between outlet 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 CO2Device, it is characterised in that：The liquefied ammonia EGR
Pipeline between the outlet of middle ammonia storage tank (25) and the shell side of the first condenser (15) is provided with the tenth valve (41), the first condenser
(15) pipeline between shell-side outlet and refrigeration unit (26) is provided with the 11st valve (42), and refrigeration unit (26) is cold with the 3rd
Pipeline between the shell side of condenser (27) is provided with the 12nd valve (43), outlet and the ammonia storage tank of the shell side of the 3rd condenser (27)
(25) the pipeline between import is provided with the 13rd valve (44).
8. oil field according to claim 1 helps and adopts tail gas recycle CO2Device, it is characterised in that：The water circle device is cool
Pipeline between the delivery port and water pump (29) of water tower (28) is provided with the 14th valve (45), water pump (29) respectively with three stage compression
The cylinder of machine (2), 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) and
The 15th valve (46), the 16th valve (47), the 17th valve are respectively equipped with pipeline between the tube side of three condensers (27)
Door (48), the 18th valve (49) and the 19th valve (50)；The cylinder outlet of three-stage blower (2), the first water cooler (3)
Shell-side outlet, the shell-side outlet of the second water cooler (30), the shell-side outlet of the 3rd water cooler (31) and the 3rd condenser (27)
Tube side outlet is respectively equipped with the 20th valve (51), the 21st valve with the pipeline between the water inlet of cooling tower (28) respectively
Door (52), the 22nd valve (53), the 23rd valve (54) and the 24th valve (55).
9. a kind of oil field helps and adopts tail gas recycle CO2Technique, it is characterised in that：The technique is to be divided into unstripped gas separation method, liquefied ammonia
Circulating cooling method and water circulation cooling means：
A, unstripped gas separation method：
Step one：Unstripped gas is set to enter in surge tank (1), the main component of its unstripped gas is：Nitrogen, carbon dioxide, methane, second
Alkane, water and light crude oil, its pressure are 0.5Mpa, and temperature is normal temperature；
Step 2：Compression unstripped gas：The unstripped gas for entering surge tank in step one is set to sequentially enter the one-level of three-stage blower (2)
Compression section, the tube side of the second water cooler (30), two-stage compression workshop section, the tube side of the 3rd water cooler (31) and three stage compression workshop section
Interior, when outlet of the unstripped gas in three-stage blower (2), its pressure is 5.0Mpa, and temperature is 75 DEG C；
Step 3：Separate light crude oil：The unstripped gas exported by three-stage blower (2) in step 2 is set to pass sequentially through the first water
First reboiler (5) of the tube side of cooler (3) and first rectifying column (4) bottom enters in first rectifying column (4), and unstripped gas is the
By rectifying in one rectifying column (4), high boiling substance is set to enter first rectifying column (4) bottom, high boiling substance passes through the first liquid
Mutually outlet (6) enters light crude oil and reclaims in storage tank (7), and low-boiling point material is gone out by the gaseous mixture at the top of first rectifying column (4)
Mouth (11) enters in the second reboiler (13)；The unstripped gas is by temperature after the tube side of the first water cooler (3)：60 DEG C, institute
State unstripped gas is by the temperature after the first reboiler (5)：40 DEG C, the unstripped gas passes through rectifying in first rectifying column (4)
The ratio of high boiling substance and low-boiling point material is 23: 77 after separation, and the light crude oil is reclaimed and include in storage tank (7) lightweight original
Oil, carbon dioxide and water, wherein, carbon dioxide accounts for 4% of carbon dioxide in surge tank (1) interior unstripped gas, and water accounts for surge tank (1)
More than the 99% of interior unstripped gas reclaimed water, light crude oil is the light crude oil of whole in surge tank (1) interior unstripped gas；The low boiling
Include nitrogen, carbon dioxide, methane and ethane in material；
Step 4：It is more than 97% that purifying carbon dioxide to concentration will be reclaimed：Make to separate the raw material after light crude oil in step 3
Gas sequentially passes through the second reboiler (13) liquid-phase outlet (9), the tube side import of the first condenser (15), the first condenser (15)
Tube side export, then respectively enter first rectifying column (4) phegma import (14) and Second distillation column (12) in the middle part of backflow
In liquid import (16)；The unstripped gas of the phegma import (14) of the entrance first rectifying column (4) again passes by first rectifying column
(4) rectifying is carried out, high boiling substance is entered first rectifying column (4) bottom, high boiling substance is entered by the first liquid-phase outlet (6)
Enter light crude oil to reclaim in storage tank (7), low-boiling point material enters the by the mixed gas outlet (11) at the top of first rectifying column (4)
In two reboilers (13)；The unstripped gas in phegma import (16) in the middle part of the entrance Second distillation column (12) is by the second essence
Tower (12) rectifying is evaporated, the high boiling substance after rectifying enters Second distillation column (12) bottom, and by Second distillation column (12) bottom
Portion sequentially enters the tube side and liquid CO of subcooler (18)2In storage tank (19), low-boiling point material is pushed up by Second distillation column (12)
Incoagulable gas outlet (21) in portion enters the shell side of the second condenser (20)；It is described by after Second distillation column (12) rectifying
High boiling substance includes the carbon dioxide that concentration is more than 97%, balance of ethane, and its temperature is 0 DEG C；It is described smart by second
Evaporating the low-boiling point material after tower (12) rectifying includes 50% carbon dioxide and 35% methane, balance of ethane, by second
The methane in low-boiling point material after rectifying column (12) rectifying is methane whole in unstripped gas described in step one；
Step 5：Product is subcooled：The tube side and liquid CO of subcooler (18)2Pipeline between storage tank (19) is provided with threeway, above-mentioned
Tube side by the high boiling substance after Second distillation column (12) rectifying by subcooler (18) and threeway described in step 4, the
Six valves (37), the tube side of the second condenser (20) and the shell side of subcooler (18) enter surge tank (1) and three-stage blower (2)
Between pipeline in；The temperature by high boiling substance after the tube side of subcooler (18) is -4 DEG C；It is described by subcooler
(18) tube side and threeway, through the 6th valve (37) throttling to 0.7Mpa, temperature is -49.5 DEG C；By the second condenser (20)
Tube side heat exchange after temperature be increased to -22.9 DEG C, its by subcooler (18) shell side heat exchange after temperature be -2 DEG C；
Step 6：Separation of methane：Pass through second by the low-boiling point material after Second distillation column (12) rectifying described in step 4
The shell side of condenser (20) enters in gas-liquid separator (22) carries out gas-liquid separation, and the gas after gas-liquid separation passes through gas-liquid separation
Gaseous phase outlet at the top of device (22) enters in incoagulable gas recycling can (24), and its liquid is by gas-liquid separator (22) bottom
The phegma import (23) on liquid-phase outlet and Second distillation column (12) top enters in Second distillation column (12), and liquid is in the second essence
Evaporating in tower (12) carries out rectifying separation, and the high boiling substance after separation enters Second distillation column (12) bottom, and by the second essence
Evaporate tube side and liquid CO that tower (12) bottom sequentially enters subcooler (18)2In storage tank (19), low-boiling point material is by the second essence
The shell side that incoagulable gas outlet (21) at the top of tower (12) enters the second condenser (20) is evaporated, repetition enters gas-liquid separator
(22) gas-liquid separation is carried out in；The composition of the gas after gas-liquid separation is 67.6% carbon dioxide, balance of methane and ethane；
Gas in the incoagulable gas recycling can (24) as pressure-variable adsorption methane device source of the gas；
B, liquefied ammonia circulating cooling method：
Step one：By the liquefied ammonia in ammonia storage tank (25) by the tenth valve (41) reducing pressure by regulating flow to 0.1MPa, temperature is：- 33 DEG C,
Into in the shell side of the first condenser (15), the unstripped gas after light crude oil is separated in method and step four with above-mentioned raw materials qi leel
Exchanged heat；
Step 2：Make shell-side outlet and refrigeration of the liquefied ammonia in above-mentioned first condenser (15) shell side by the first condenser (15)
Unit (26) enters in the shell side of the 3rd condenser (27), and is exchanged heat with the industry water in the 3rd condenser (27) tube side,
Liquefied ammonia pressure after heat exchange is：1.6MPa, its temperature is：40℃；
Step 3：Make liquefied ammonia in above-mentioned 3rd condenser (27) shell side by the circumfluence of ammonia storage tank (25) to ammonia storage tank
(25) in；
C, water circulation cooling means：
Step one：The industry water in cooling tower (28) is set to be forced into by water pump (29)：0.3Mpa~0.4Mpa, water temperature is：35
℃；
Step 2：Make the industry water after pressurization that the cylinder of three-stage blower (2), the first water cooler (3) are respectively enterd by pipeline
Shell side, the shell side of the second water cooler (30), in the tube side of the shell side of the 3rd water cooler (31) and the 3rd condenser (27), respectively
Cylinder, the shell side of the first water cooler (3) to three-stage blower (2), the shell side of the second water cooler (30), the 3rd water cooler (31)
Shell side and the tube side of the 3rd condenser (27) carry out heat exchange cooling, the water temperature after its heat exchange cooling is：36℃；
Step 3：Make to enter in cooling tower (28) by pipeline respectively by the industry water after the cooling that exchanges heat in step 2, circulation
Use.
10. oil field according to claim 9 helps and adopts tail gas recycle CO2Technique, it is characterised in that：The unstripped gas is separated
In method and step two, the unstripped gas of surge tank is set to enter in the tube side of the second water cooler (30) by the first valve (32)；It is described
In unstripped gas separation method step 3, the unstripped gas of three-stage blower (2) outlet enters the first rectifying by the second valve (33)
In first reboiler (5) of tower (4) bottom.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510117712.6A CN104748506B (en) | 2015-03-13 | 2015-03-13 | Device for recycling CO2 from oil field mining assisting tail gas and process thereof |
Applications Claiming Priority (1)
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| CN105502394B (en) * | 2015-12-17 | 2017-07-14 | 江苏华扬液碳有限责任公司 | A kind of gas field carbon dioxide prepares industrial liquid carbon dioxide separation purification system |
| CN106744956A (en) * | 2016-12-22 | 2017-05-31 | 乐陵胜利新能源有限责任公司 | A kind of high-pressure washing methane purification carbon dioxide in process recovery process |
| CN107345736B (en) * | 2017-05-24 | 2022-08-30 | 杭氧集团股份有限公司 | H 2 Low-temperature separation device for S |
| CN108640810A (en) * | 2018-07-12 | 2018-10-12 | 中国石油大学(华东) | CO in associated gas2-C2H6The extraction separating method and system of azeotropic mixture |
| CN110195962A (en) * | 2019-06-05 | 2019-09-03 | 杭州凯德空分设备有限公司 | Rubbish landfill gas, biogas or chemical industry tail gas extract high-purity carbon dioxide process equipment |
| CN110440526A (en) * | 2019-07-27 | 2019-11-12 | 江西江氨科技有限公司 | Food-grade carbon-dioxide preparation system |
| WO2021016779A1 (en) * | 2019-07-27 | 2021-02-04 | 江西江氨科技有限公司 | Food-grade co2 preparation system |
| CN111675220B (en) * | 2020-05-08 | 2023-06-27 | 江西江氨科技有限公司 | CO-containing in tail gas from carbonate production 2 Extraction and refining system |
| CN111977654B (en) * | 2020-10-21 | 2024-05-24 | 重庆瑞信气体有限公司 | CO is retrieved in low temperature methanol washing workshop section2Is a device and process thereof |
| CN114791205B (en) * | 2022-04-22 | 2023-07-21 | 杭州特盈能源技术发展有限公司 | Green electricity high-efficiency conversion low-energy consumption air separation energy storage and CO 2 Purification liquefaction process |
| CN116518648B (en) * | 2023-05-08 | 2023-11-17 | 环西汀新材料(江苏)有限公司 | Liquefied petroleum gas separation treatment system and treatment process |
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| US4332598A (en) * | 1980-11-13 | 1982-06-01 | Air Products And Chemicals, Inc. | Process for treating industrial gas stream |
| US4595404A (en) * | 1985-01-14 | 1986-06-17 | Brian J. Ozero | CO2 methane separation by low temperature distillation |
| US4720294A (en) * | 1986-08-05 | 1988-01-19 | Air Products And Chemicals, Inc. | Dephlegmator process for carbon dioxide-hydrocarbon distillation |
| CN202246075U (en) * | 2011-08-05 | 2012-05-30 | 化学工业第二设计院宁波工程有限公司 | System for producing food-grade carbon dioxide by utilizing temperature-rising vaporization cold energy of low-temperature ethylene |
| CN102853634A (en) * | 2012-08-14 | 2013-01-02 | 中国石油化工股份有限公司 | Method for recovering carbon dioxide |
| CN103691250B (en) * | 2013-10-19 | 2016-04-06 | 盘锦道博尔石油新技术开发有限公司 | The method for purifying and recovering of time anger in a kind of steam drive oil production |
| CN204513905U (en) * | 2015-03-13 | 2015-07-29 | 河南心连心深冷能源股份有限公司 | Oil field helps adopts tail gas recycle CO 2device |
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