CN114852973A - Method and system for synchronously preparing nitrogen and carbon dioxide from oil field boiler flue gas - Google Patents
Method and system for synchronously preparing nitrogen and carbon dioxide from oil field boiler flue gas Download PDFInfo
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- CN114852973A CN114852973A CN202210627996.3A CN202210627996A CN114852973A CN 114852973 A CN114852973 A CN 114852973A CN 202210627996 A CN202210627996 A CN 202210627996A CN 114852973 A CN114852973 A CN 114852973A
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- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 354
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 title claims abstract description 280
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 179
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 177
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 93
- 239000003546 flue gas Substances 0.000 title claims abstract description 93
- 238000000034 method Methods 0.000 title claims abstract description 41
- JCXJVPUVTGWSNB-UHFFFAOYSA-N nitrogen dioxide Inorganic materials O=[N]=O JCXJVPUVTGWSNB-UHFFFAOYSA-N 0.000 title claims abstract description 27
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 124
- 238000000926 separation method Methods 0.000 claims abstract description 88
- CKUAXEQHGKSLHN-UHFFFAOYSA-N [C].[N] Chemical compound [C].[N] CKUAXEQHGKSLHN-UHFFFAOYSA-N 0.000 claims abstract description 61
- 238000000746 purification Methods 0.000 claims abstract description 48
- 239000007788 liquid Substances 0.000 claims abstract description 36
- 238000011282 treatment Methods 0.000 claims abstract description 17
- 238000005406 washing Methods 0.000 claims description 32
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 22
- 238000003860 storage Methods 0.000 claims description 20
- 229910052799 carbon Inorganic materials 0.000 claims description 16
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 15
- 229910001873 dinitrogen Inorganic materials 0.000 claims description 7
- 238000001816 cooling Methods 0.000 claims description 5
- 238000001035 drying Methods 0.000 claims description 4
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 claims description 2
- 239000007789 gas Substances 0.000 abstract description 49
- 238000004519 manufacturing process Methods 0.000 abstract description 8
- 238000002347 injection Methods 0.000 abstract description 7
- 239000007924 injection Substances 0.000 abstract description 7
- 230000008569 process Effects 0.000 abstract description 7
- 239000002994 raw material Substances 0.000 abstract description 4
- 101100456566 Caenorhabditis elegans dpy-22 gene Proteins 0.000 description 5
- 238000010793 Steam injection (oil industry) Methods 0.000 description 5
- 239000012528 membrane Substances 0.000 description 5
- 238000011084 recovery Methods 0.000 description 5
- 239000000126 substance Substances 0.000 description 5
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 4
- 239000000498 cooling water Substances 0.000 description 4
- 238000011161 development Methods 0.000 description 4
- 238000005265 energy consumption Methods 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 239000001301 oxygen Substances 0.000 description 4
- 229910052760 oxygen Inorganic materials 0.000 description 4
- 238000007906 compression Methods 0.000 description 3
- 230000006835 compression Effects 0.000 description 3
- 238000006073 displacement reaction Methods 0.000 description 3
- 238000000605 extraction Methods 0.000 description 3
- 238000004458 analytical method Methods 0.000 description 2
- 239000003814 drug Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 101150107050 PSA2 gene Proteins 0.000 description 1
- 239000003463 adsorbent Substances 0.000 description 1
- 150000001412 amines Chemical class 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 230000003749 cleanliness Effects 0.000 description 1
- 239000002131 composite material Substances 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000011070 membrane recovery Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000002808 molecular sieve Substances 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000002203 pretreatment Methods 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 230000009919 sequestration Effects 0.000 description 1
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
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Classifications
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B21/00—Nitrogen; Compounds thereof
- C01B21/04—Purification or separation of nitrogen
- C01B21/0405—Purification or separation processes
- C01B21/0433—Physical processing only
- C01B21/045—Physical processing only by adsorption in solids
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B32/00—Carbon; Compounds thereof
- C01B32/50—Carbon dioxide
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0257—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of nitrogen
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0266—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of carbon dioxide
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2
Abstract
The invention discloses a method and a system for synchronously preparing nitrogen and carbon dioxide from oil field boiler flue gas, which relate to the field of oil field boiler flue gas treatment and comprise the following steps: s101: pretreating the flue gas; s102: performing PSA carbon-nitrogen separation on the flue gas after the flue gas pretreatment; the nitrogen after PSA carbon nitrogen separation is processed by S103, and the carbon dioxide after separation is processed by S104; s103: PSA carbon-nitrogen separation residual pressure is utilized, and PSA nitrogen purification is carried out on the separated nitrogen to obtain high-concentration nitrogen; s104: and compressing the separated carbon dioxide, and then rectifying and purifying to obtain liquid carbon dioxide. In the process of capturing carbon dioxide, nitrogen in the tail gas is enriched and is used as raw material gas for nitrogen separation, so that the separation efficiency is improved, and the production cost is reduced; compared with the traditional method, the method can continuously and stably provide high-quality carbon dioxide and nitrogen, and meets the requirement of gas injection purity.
Description
Technical Field
The invention relates to the field of treatment of flue gas of an oil field boiler, in particular to a system for synchronously preparing nitrogen and carbon dioxide from flue gas of the oil field boiler.
Background
Worldwide, the gas injection oil displacement technology has become the first enhanced oil recovery technology with the production scale. According to the analysis of oil extraction and energy consumption of each oil extraction plant in the Xinjiang oil field, the thickened oil consumes 87% of energy with 33% of yield, the thickened oil is exploited with 92% of energy consumption for thermal recovery and steam injection, the main energy consumption of the Xinjiang oil field in the thermal recovery of the thickened oil can be seen, and the carbon emission is mainly from tail gas of a steam injection boiler. In a gas flooding technical system, carbon dioxide flooding can realize carbon sequestration while oil displacement and utilization, and has economic and environmental benefits; the nitrogen flooding has the characteristics of high compression expansibility and poor gas heat conductivity, and is widely applied to the fields of miscible flooding, immiscible flooding and the like. Generally, high-quality carbon dioxide and nitrogen gas sources are concentrated in a chemical area, are far away from an oil field gas injection area, and have high conveying cost. With the increase of the exploitation time limit of the oil field and the reduction of the oil-gas ratio, development modes face conversion, low-cost nitrogen and carbon dioxide are needed for later oil extraction gas drive and compound drive development, and how to obtain the low-cost nitrogen and carbon dioxide becomes a main factor restricting the development of the gas drive technology.
Chinese invention patent CN107899376A discloses a combined capturing and recovering device and method for carbon dioxide and nitrogen in flue gas, the device comprises a flue gas treatment system, a first C02 membrane separation unit, a second C02 membrane separation unit and an N2 membrane separation unit. The device belongs to a membrane recovery mode, can trap carbon dioxide and nitrogen at the same time, but has low product purity, high requirement on air source cleanliness of the membrane, easy blockage in the using process of equipment, inconvenient maintenance after blockage, short service life and higher price of the membrane, and is not suitable for industrial application.
The Chinese patent CN110498416A discloses a system for synchronously recovering carbon dioxide and nitrogen from boiler flue gas of a coal-fired power plant, which comprises a flue gas pretreatment system, a PSA1 system, a PSA2 system, a carbon dioxide compression and purification system, a carbon dioxide rectification and storage system and a PSA high-purity nitrogen preparation system. Although the system can capture carbon dioxide and nitrogen to a large extent, the system has the problems of inflexible equipment operation, high energy consumption and low carbon dioxide recovery rate. When the nitrogen yield of the later stage is reduced or the nitrogen is not trapped, the pressure compression value of the former stage is too high, and the power consumption is large.
Chinese patent CN113975950A discloses a system and a method for synchronously recovering carbon dioxide and nitrogen in flue gas by a chemical method and a PSA method, wherein the system and the method synchronously recover the carbon dioxide and nitrogen in the flue gas by the chemical method and the PSA method, and comprise a carbon dioxide chemical method recovery system, a carbon dioxide refining and liquefying system and a nitrogen PSA concentration and purification system. The method uses a chemical amine method to perform carbon-nitrogen separation, a large amount of steam is consumed in the process, the steam produced by the oil field gas boiler is used for steam injection and oil displacement, the steam consumption influences the steam yield of the gas boiler, and the process is not suitable for the oil field gas boiler.
Therefore, it is desirable to provide a method and system for synchronously producing nitrogen and carbon dioxide from oilfield boiler flue gas, which solves the above-mentioned deficiencies of the prior art.
Disclosure of Invention
In view of the above defects of the prior art, the technical problem to be solved by the invention is how to obtain high-quality carbon dioxide and nitrogen with low cost for gas injection flooding.
In order to realize the aim, the invention provides a method for synchronously preparing nitrogen and carbon dioxide from oil field boiler flue gas, which comprises the following steps:
s101: pretreating the flue gas; carrying out pretreatment, temperature reduction, pressurization, drying and other treatments on tail gas from an oil field gas boiler;
s102: performing PSA carbon-nitrogen separation on the flue gas after the flue gas pretreatment; the nitrogen after PSA carbon nitrogen separation is processed by S103, and the carbon dioxide after separation is processed by S104;
s103: PSA carbon-nitrogen separation residual pressure is utilized, PSA nitrogen purification is carried out on the separated nitrogen, high-concentration nitrogen is obtained, and the nitrogen purity is more than 99%;
s104: and compressing the separated carbon dioxide, and then rectifying and purifying to obtain liquid carbon dioxide with the purity of more than 99.5%.
In order to achieve the above object, another aspect of the present invention provides a method for synchronously producing nitrogen and carbon dioxide from flue gas of an oilfield boiler, comprising the following steps:
s201: pretreating flue gas, cooling by a water washing tower, pressurizing by a compressor, dehydrating by a drier, and then keeping the pressure higher than 0.8MPa, the temperature lower than 40 ℃ and the dew point temperature lower than 30 ℃;
s202: performing PSA carbon-nitrogen separation on the flue gas after the flue gas pretreatment; performing S203 on the medium-concentration nitrogen after PSA carbon-nitrogen separation, and performing S204 on the medium-concentration carbon dioxide after PSA carbon-nitrogen separation;
s203: PSA carbon-nitrogen separation residual pressure is utilized, PSA nitrogen purification is carried out on the separated medium-concentration nitrogen to obtain high-concentration nitrogen, the high-concentration nitrogen is product nitrogen, and the nitrogen purity is more than 99%;
s204: the separated medium-concentration carbon dioxide is pressurized again through a PSA compressor, the carbon dioxide is sent to a PSA for purification, and the separated high-concentration carbon dioxide is S205; the separated nitrogen is merged with the medium-concentration nitrogen separated from the PSA carbon nitrogen, and S203 is carried out;
s205: and compressing the separated high-concentration carbon dioxide, and then sending the compressed high-concentration carbon dioxide into a rectifying system with a refrigerating function for rectifying and purifying to obtain liquid carbon dioxide with the purity of more than 99.5 percent.
Preferably, the pre-treatment of the flue gas comprises subjecting the tail gas from an oil field gas boiler to at least one of: washing; cooling; supercharging; and (5) drying.
In order to achieve the purpose, the invention provides a system for synchronously preparing nitrogen and carbon dioxide from oil field boiler flue gas, wherein the nitrogen and carbon dioxide are synchronously prepared by adopting any one of the two methods.
In order to achieve the above object, the present invention further provides a system for synchronously producing nitrogen and carbon dioxide from flue gas of an oilfield boiler, which is characterized by comprising:
a carbon-nitrogen separation unit: separating nitrogen and carbon dioxide;
flue gas pretreatment unit: the flue gas entering the carbon-nitrogen separation unit is pretreated before the carbon-nitrogen separation unit;
a nitrogen treatment unit: the nitrogen gas treatment device is positioned behind the carbon and nitrogen separation unit and is used for treating nitrogen gas generated by the carbon and nitrogen separation unit; and
a carbon dioxide treatment unit: and the carbon and nitrogen separation unit is positioned behind the carbon and nitrogen separation unit and is used for treating the carbon dioxide generated by the carbon and nitrogen separation unit.
Preferably, the flue gas pretreatment unit comprises: the device comprises a water washing tower, a circulating pump, a cooler, a flue gas compressor and a dryer; the inlet at the bottom of the washing tower is flue gas to be treated, the inlet at the upper part of the washing tower is connected with the outlet of the cooler, the outlet at the bottom of the washing tower is connected with the inlet of the circulating pump, and the outlet at the upper part of the washing tower is connected with the inlet of the flue gas compressor; the outlet of the circulating pump is connected with the inlet of the cooler; the inlet of the dryer is connected with the outlet of the flue gas compressor, and the outlet of the dryer is connected with the carbon-nitrogen separation unit.
Preferably, the carbon and nitrogen separation unit comprises: carbon nitrogen separation PSA, PSA compressor and carbon dioxide purification PSA; the inlet of the carbon-nitrogen separation PSA is connected with the flue gas pretreatment unit, the lower outlet of the carbon-nitrogen separation PSA is connected with the inlet of the PSA compressor, and the upper outlet of the carbon-nitrogen separation PSA is mixed with the upper outlet of the carbon dioxide purification PSA and then connected with the nitrogen treatment unit; the outlet of the PSA compressor is connected with the inlet of the carbon dioxide purification PSA; and the lower inlet of the carbon dioxide purification PSA is connected with a carbon dioxide treatment unit.
Preferably, the nitrogen treatment unit is a nitrogen purification PSA, the inlet of the nitrogen purification PSA is nitrogen generated by the carbon and nitrogen separation unit, the top outlet is low-concentration nitrogen, and the bottom outlet is product nitrogen.
Preferably, the carbon dioxide processing unit comprises: the system comprises a rectification compressor, a precooler, a rectification tower and a liquid carbon dioxide storage tank; the inlet of the rectification compressor is carbon dioxide generated by the carbon-nitrogen separation unit, and the outlet of the rectification compressor is connected with the first inlet of the precooler; the first outlet of the precooler is connected with the inlet of the rectifying tower, and the second outlet of the rectifying compressor is precooled and recycled low-concentration carbon dioxide; the second inlet of the rectification compressor is connected with the outlet at the upper part of the rectification tower; an outlet at the upper part of the rectifying tower is connected with an inlet of the liquid carbon dioxide storage tank; and the outlet of the liquid carbon dioxide storage tank is product liquid carbon dioxide.
In order to achieve the above object, the present invention further provides a system for synchronously producing nitrogen and carbon dioxide from flue gas of an oilfield boiler, comprising: the system comprises a water washing tower, a circulating pump, a cooler, a flue gas compressor, a dryer, a carbon-nitrogen separation PSA, a PSA compressor, a carbon dioxide purification PSA, a nitrogen purification PSA, a rectification compressor, a precooler, a rectification tower and a liquid carbon dioxide storage tank; the inlet at the bottom of the washing tower is flue gas to be treated, the inlet at the upper part of the washing tower is connected with the outlet of the cooler, the outlet at the bottom of the washing tower is connected with the inlet of the circulating pump, and the outlet at the upper part of the washing tower is connected with the inlet of the flue gas compressor; the outlet of the circulating pump is connected with the inlet of the cooler; the inlet of the dryer is connected with the outlet of the flue gas compressor; the inlet of the carbon-nitrogen separation PSA is connected with the outlet of the dryer, the lower outlet of the carbon-nitrogen separation PSA is connected with the inlet of the PSA compressor, and the upper outlet of the carbon-nitrogen separation PSA is mixed with the upper outlet of the carbon dioxide purification PSA and then connected with the inlet of the nitrogen purification PSA (9); the outlet of the PSA compressor is connected with the inlet of the carbon dioxide purification PSA; the inlet of the rectification compressor is connected with the lower outlet of the PSA, and the outlet of the rectification compressor is connected with the first inlet of the precooler; the first outlet of the precooler is connected with the inlet of the rectifying tower, and the second outlet of the rectifying compressor is precooled and recycled low-concentration carbon dioxide; a second inlet of the rectification compressor is connected with an outlet at the upper part of the rectification tower; an outlet at the upper part of the rectifying tower is connected with an inlet of the liquid carbon dioxide storage tank; the outlet of the liquid carbon dioxide storage tank is product liquid carbon dioxide; the top outlet of the nitrogen purification PSA is low-concentration nitrogen, and the bottom outlet is product nitrogen.
According to the method and the system for synchronously preparing the nitrogen and the carbon dioxide from the flue gas of the oil field gas boiler, provided by the invention, in the carbon dioxide trapping process, the nitrogen in the tail gas is enriched and is used as the raw material gas for nitrogen separation, so that the separation efficiency is improved, and the production cost is reduced; compared with the traditional method, the method can continuously and stably provide high-quality carbon dioxide and nitrogen, and meet the requirement of gas injection purity; the production device of the system is arranged on the oil field, and the rear end of the oil field gas boiler is closer to the well mouth, so that the conveying cost is reduced.
The conception, specific structure and technical effects of the present invention will be further described in conjunction with the accompanying drawings to fully understand the purpose, characteristics and effects of the present invention.
Drawings
Fig. 1 is a system structure diagram corresponding to the third embodiment of the present invention.
In the figure:
1. washing the tower with water;
2. a circulation pump;
3. a cooler;
4. a flue gas compressor;
5. a dryer;
6. carbon nitrogen separation PSA;
7. a PSA compressor;
8. purifying PSA by carbon dioxide;
9. PSA purification by nitrogen;
10. a rectification compressor;
11. a precooler;
12. a rectifying tower;
13. a liquid carbon dioxide storage tank.
Detailed Description
The technical contents of the preferred embodiments of the present invention will be made clear and easily understood by referring to the drawings attached to the specification. The present invention may be embodied in many different forms of embodiments and the scope of the invention is not limited to the embodiments set forth herein.
In the drawings, structurally identical elements are represented by like reference numerals, and structurally or functionally similar elements are represented by like reference numerals throughout the several views. The size and thickness of each component shown in the drawings are arbitrarily illustrated, and the present invention is not limited to the size and thickness of each component. The thickness of the components may be exaggerated where appropriate in the figures to improve clarity.
Example one
The method for synchronously preparing nitrogen and carbon dioxide from the flue gas of the oil field boiler comprises the following steps:
flue gas pretreatment, namely pretreating tail gas from an oil field gas boiler for cooling, pressurizing and drying, and sending the tail gas into PSA carbon nitrogen separation;
performing PSA carbon-nitrogen separation on the flue gas from the flue gas pretreatment, feeding the separated nitrogen into PSA nitrogen for purification, and feeding the separated carbon dioxide into carbon dioxide for rectification and liquefaction;
PSA nitrogen purification is carried out by utilizing the residual pressure from PSA carbon-nitrogen separation, the purified low-concentration nitrogen is discharged, and the purity of the high-concentration nitrogen of the product is more than 99 percent;
compressing the separated carbon dioxide, and then sending the compressed carbon dioxide into a rectifying system with a refrigerating function for rectifying and purifying, emptying the purified low-concentration carbon dioxide, wherein the product is liquid carbon dioxide and the purity is more than 99.5%;
sending the carbon dioxide to a carbon dioxide storage and transportation tank for storing and transporting liquid carbon dioxide generated by rectifying and liquefying carbon dioxide.
In the carbon dioxide trapping process of the method, nitrogen in the tail gas is enriched and is used as raw material gas for nitrogen separation, so that the separation efficiency is improved, and the production cost is reduced; compared with the traditional method, the method can continuously and stably provide high-quality carbon dioxide and nitrogen, and meet the requirement of gas injection purity; the production device is arranged on the oil field, and the rear end of the oil field gas boiler is close to the well mouth, so that the conveying cost is reduced.
Example two
The method for synchronously preparing nitrogen and carbon dioxide from the flue gas of the oil field boiler comprises the following steps:
the flue gas from the oil field gas boiler contains carbon dioxide, nitrogen, oxygen and the like;
flue gas from an oil field gas boiler enters flue gas pretreatment, and is cooled by a washing tower, pressurized by a compressor and dehydrated by a drier, and then the pressure is more than 0.8MPa, the temperature is lower than 40 ℃, and the dew point temperature is lower than-30 ℃;
flue gas from a flue gas pretreatment gas boiler enters PSA carbon nitrogen separation;
the separated medium-concentration carbon dioxide is pressurized again by a PSA compressor, and is sent to carbon dioxide for purification PSA, and the separated high-concentration carbon dioxide is sent to carbon dioxide for rectification and liquefaction; the separated high-concentration nitrogen is converged with the high-concentration nitrogen separated by the carbon-nitrogen separation PSA and sent to the nitrogen purification PSA;
introducing middle-concentration nitrogen from PSA carbon-nitrogen separation into nitrogen to purify PSA, emptying the separated low-concentration nitrogen, wherein the high-concentration nitrogen is product gas, and the purity of the nitrogen is more than 99%;
high-concentration carbon dioxide from carbon-nitrogen separation is sent into a rectification system through a rectification compressor under the pressure increase;
precooling carbon dioxide pressurized by a rectification compressor by a rectification system and then sending the carbon dioxide into a rectification tower;
rectifying the carbon dioxide from the precooling in a rectifying tower, sending the separated low-concentration carbon dioxide into a precooler to recover cold energy and then discharging the carbon dioxide to the air, and sending the separated liquid carbon dioxide into a liquid carbon dioxide storage tank;
the liquid carbon dioxide generated from the rectifying tower is stored and then is output as the product liquid carbon dioxide, the pressure is 0.7MPa, the temperature is-23 ℃, and the purity is more than 99.5 percent.
In the carbon dioxide trapping process of the method, nitrogen in the tail gas is enriched and is used as raw material gas for nitrogen separation, so that the separation efficiency is improved, and the production cost is reduced; compared with the traditional method, the method can continuously and stably provide high-quality carbon dioxide and nitrogen, and meet the requirement of gas injection purity; the production device is arranged on the oil field, and the rear end of the oil field gas boiler is close to the well mouth, so that the conveying cost is reduced.
EXAMPLE III
As shown in fig. 1, a system for synchronously producing nitrogen and carbon dioxide from flue gas of an oilfield boiler comprises: the system comprises a water washing tower 1, a circulating pump 2, a cooler 3, a flue gas compressor 4, a dryer 5, a carbon-nitrogen separation PSA6, a PSA compressor 7, a carbon dioxide purification PSA8, a nitrogen purification PSA9, a rectification compressor 10, a precooler 11, a rectification tower 12 and a liquid carbon dioxide storage tank 13;
the inlet at the bottom of the water washing tower 1 is flue gas to be treated;
an inlet at the upper part of the water washing tower 1 is connected with an outlet of the cooler 3, an outlet at the bottom of the water washing tower 1 is connected with an inlet of the circulating pump 2, and an outlet at the upper part of the water washing tower 1 is connected with an inlet of the flue gas compressor 4;
the outlet of the circulating pump 2 is connected with the inlet of the cooler 3;
the inlet of the dryer 5 is connected with the outlet of the flue gas compressor 4;
an inlet of the carbon-nitrogen separation PSA6 is connected with an outlet of the dryer 5, a lower outlet of the carbon-nitrogen separation PSA6 is connected with the PSA compressor 7, an upper outlet of the carbon-nitrogen separation PSA6 is mixed with an upper outlet of the carbon dioxide purification PSA8 and then is connected with the nitrogen purification PSA 9;
the outlet of the PSA compressor 7 is connected with the inlet of the carbon dioxide purification PSA 8;
the inlet of the rectification compressor 10 is connected with the outlet at the lower part of the carbon dioxide purification PSA8, and the outlet of the rectification compressor 10 is connected with the first inlet of the precooler 11;
a first outlet of the precooler 11 is connected with an inlet of the rectifying tower 12, and a second outlet of the rectifying compressor 10 is precooled and recycled low-concentration carbon dioxide; a second inlet of the rectification compressor 10 is connected with an outlet at the upper part of the rectification tower 12;
an outlet at the upper part of the rectifying tower 12 is connected with an inlet of a liquid carbon dioxide storage tank 13;
the outlet of the liquid carbon dioxide storage tank 13 is the product liquid carbon dioxide;
the inlet of the nitrogen purification PSA9 is nitrogen generated by a carbon-nitrogen separation unit, the top outlet is low-concentration nitrogen, and the bottom outlet is product nitrogen.
In this embodiment, the water scrubber 1 is specifically a sieve plate spray tower; the flue gas compressor 4 is specifically a screw compressor, and the parameter Q is 10000m 3 The amount of the Pc is 2, and the Pc is 1.0MPa and is used for standby at one time in daily life; the processing capacity Q of the dryer 5 is 10000m 3 The amount of the medicine is 2, and the medicine is used for one day and is prepared for another day.
The functions of the modules are described in detail below with reference to fig. 1:
flue gas from an oil field gas boiler contains carbon dioxide, nitrogen, oxygen and the like, wherein the content of the carbon dioxide is 7.9mol percent, and the content of the nitrogen is 72.9mol percent;
the inlet of the water washing tower 1 is gas boiler flue gas, the outlet at the bottom is high-temperature circulating cooling water, and the outlet at the top is cooled gas boiler flue gas;
the inlet of the circulating pump 2 is high-temperature circulating cooling water at the bottom of the washing tower, and the outlet of the circulating pump is pressurized high-temperature circulating cooling water;
the inlet of the cooler 3 is high-temperature circulating cooling water, and the outlet of the cooler 3 is low-temperature cooling circulating water;
the inlet of the flue gas compressor 4 is cooled flue gas of the gas-fired boiler;
the inlet of the dryer 5 is pressurized gas boiler flue gas;
the carbon-nitrogen separation PSA6 comprises dried flue gas from a gas-fired boiler at the inlet, medium-concentration nitrogen at the top outlet and medium-concentration carbon dioxide at the bottom outlet;
the inlet of the PSA compressor 7 is medium-concentration carbon dioxide, and the outlet is pressurized medium-concentration carbon dioxide;
the carbon dioxide purification PSA8 comprises pressurized medium-concentration carbon dioxide at the inlet, medium-concentration nitrogen at the top outlet and high-concentration carbon dioxide at the bottom outlet;
nitrogen purification PSA9, wherein the inlet is medium-concentration nitrogen, the top outlet is low-concentration nitrogen, the nitrogen is directly discharged into the atmosphere, and the bottom outlet is high-concentration nitrogen;
the inlet of the rectification compressor 10 is high-concentration carbon dioxide, and the outlet of the rectification compressor is pressurized carbon dioxide;
the precooler 11 is provided with a first inlet for pressurized carbon dioxide, a first outlet for precooled carbon dioxide, a second inlet for low-concentration carbon dioxide at the top outlet of the rectifying tower and a second outlet for precooled and recycled low-concentration carbon dioxide;
an inlet of the rectifying tower 12 is precooled carbon dioxide, a top outlet is low-concentration carbon dioxide, and a bottom outlet is liquid carbon dioxide;
the inlet of the liquid carbon dioxide storage tank 13 is liquid carbon dioxide from the bottom of the rectifying tower, the outlet is product liquid carbon dioxide, the pressure is 2.4MPa, the temperature is-23 ℃, and the purity is more than 99.5%.
PSA is a novel gas separation technology, which separates gas mixtures using different gaseous molecules when separating different gas molecules using molecular sieves. The separation of nitrogen and oxygen from air is realized through the selective adsorption characteristic of the high-efficiency and high-selectivity solid adsorbent to nitrogen and oxygen.
After the device is equipped, the function of the steam injection boiler is not limited to steam supply, and the device of the invention is equipped to produce low-cost nitrogen and carbon dioxide, so that the steam injection boiler is converted into a low-carbon gas (steam) supply comprehensive station, a low-cost gas source is provided for gas drive composite steam development, and a large amount of carbon dioxide is reduced.
The foregoing detailed description of the preferred embodiments of the invention has been presented. It should be understood that numerous modifications and variations could be devised by those skilled in the art in light of the present teachings without departing from the inventive concepts. Therefore, the technical solutions available to those skilled in the art through logic analysis, reasoning and limited experiments based on the prior art according to the concept of the present invention should be within the scope of protection defined by the claims.
Claims (10)
1. A method for synchronously preparing nitrogen and carbon dioxide from oil field boiler flue gas is characterized by comprising the following steps:
s101: pretreating the flue gas;
s102: performing PSA carbon-nitrogen separation on the flue gas after the flue gas pretreatment; the nitrogen after PSA carbon nitrogen separation is processed by S103, and the carbon dioxide after separation is processed by S104;
s103: PSA carbon-nitrogen separation residual pressure is utilized, and PSA nitrogen purification is carried out on the separated nitrogen to obtain high-concentration nitrogen;
s104: and compressing the separated carbon dioxide, and then rectifying and purifying to obtain liquid carbon dioxide.
2. A method for synchronously preparing nitrogen and carbon dioxide from oil field boiler flue gas is characterized by comprising the following steps:
s201: pretreating the flue gas;
s202: performing PSA carbon-nitrogen separation on the flue gas after the flue gas pretreatment; performing S203 on the medium-concentration nitrogen after PSA carbon-nitrogen separation, and performing S204 on the medium-concentration carbon dioxide after PSA carbon-nitrogen separation;
s203: PSA carbon-nitrogen separation residual pressure is utilized, and PSA nitrogen purification is carried out on the separated medium-concentration nitrogen to obtain high-concentration nitrogen;
s204: the separated medium-concentration carbon dioxide is pressurized again through a PSA compressor, the carbon dioxide is sent to a PSA for purification, and the separated high-concentration carbon dioxide is S205; the separated nitrogen is merged with the medium-concentration nitrogen separated from the PSA carbon nitrogen, and S203 is carried out;
s205: and compressing the separated high-concentration carbon dioxide, and then sending the compressed high-concentration carbon dioxide into a rectifying system with a refrigerating function for rectifying and purifying to obtain liquid carbon dioxide.
3. The method of claim 2, wherein the pretreating flue gas comprises at least one of:
washing; cooling; supercharging; and (5) drying.
4. A system for synchronously preparing nitrogen and carbon dioxide from oil field boiler flue gas is characterized in that the nitrogen and carbon dioxide are synchronously prepared by the method of any one of claims 1 to 3.
5. The utility model provides a system for nitrogen gas and carbon dioxide are prepared in step to oil field boiler flue gas which characterized in that includes:
a carbon-nitrogen separation unit: separating nitrogen and carbon dioxide;
flue gas pretreatment unit: the flue gas entering the carbon-nitrogen separation unit is pretreated before the carbon-nitrogen separation unit;
a nitrogen treatment unit: the nitrogen gas treatment device is positioned behind the carbon and nitrogen separation unit and is used for treating nitrogen gas generated by the carbon and nitrogen separation unit; and
a carbon dioxide treatment unit: and the carbon and nitrogen separation unit is positioned behind the carbon and nitrogen separation unit and is used for treating the carbon dioxide generated by the carbon and nitrogen separation unit.
6. The system for synchronously preparing nitrogen and carbon dioxide by using the flue gas of the oilfield boiler as defined in claim 5, wherein the flue gas pretreatment unit comprises: a water washing tower (1), a circulating pump (2), a cooler (3), a flue gas compressor (4) and a dryer (5);
the inlet at the bottom of the water washing tower (1) is flue gas to be treated, the inlet at the upper part of the water washing tower (1) is connected with the outlet of the cooler (3), the outlet at the bottom of the water washing tower (1) is connected with the inlet of the circulating pump (2), and the outlet at the upper part of the water washing tower (1) is connected with the inlet of the flue gas compressor (4);
the outlet of the circulating pump (2) is connected with the inlet of the cooler (3);
the inlet of the dryer (5) is connected with the outlet of the flue gas compressor (4), and the outlet of the dryer (5) is connected with a carbon-nitrogen separation unit.
7. The system for synchronously preparing nitrogen and carbon dioxide by using the flue gas of the oilfield boiler as defined in claim 5, wherein the carbon-nitrogen separation unit comprises: carbon nitrogen separation PSA (6), PSA compressor (7) and carbon dioxide purification PSA (8);
the inlet of the carbon-nitrogen separation PSA (6) is connected with the flue gas pretreatment unit, the lower outlet of the carbon-nitrogen separation PSA (6) is connected with the PSA compressor (7), and the upper outlet of the carbon-nitrogen separation PSA (6) is mixed with the upper outlet of the carbon dioxide purification PSA (8) and then connected with the nitrogen treatment unit;
the outlet of the PSA compressor (7) is connected with the inlet of the carbon dioxide purification PSA (8);
and the lower inlet of the carbon dioxide purification PSA (8) is connected with a carbon dioxide treatment unit.
8. The system for synchronously preparing nitrogen and carbon dioxide by using the oilfield boiler flue gas as claimed in claim 5, wherein the nitrogen treatment unit is a nitrogen purification PSA (9), the inlet of the nitrogen purification PSA (9) is nitrogen generated by the carbon and nitrogen separation unit, the top outlet is low-concentration nitrogen, and the bottom outlet is product nitrogen.
9. The system for synchronously preparing nitrogen and carbon dioxide by using the flue gas of the oilfield boiler as defined in claim 5, wherein the carbon dioxide treatment unit comprises: a rectification compressor (10), a precooler (11), a rectification tower (12) and a liquid carbon dioxide storage tank (13);
the inlet of the rectification compressor (10) is carbon dioxide generated by the carbon-nitrogen separation unit, and the outlet of the rectification compressor (10) is connected with the first inlet of the precooler (11);
a first outlet of the precooler (11) is connected with an inlet of the rectifying tower (12), and a second outlet of the rectifying compressor (10) is precooled and recycled low-concentration carbon dioxide; the second inlet of the rectification compressor (10) is connected with the outlet at the upper part of the rectification tower (12);
an outlet at the upper part of the rectifying tower (12) is connected with an inlet of the liquid carbon dioxide storage tank (13);
and the outlet of the liquid carbon dioxide storage tank (13) is product liquid carbon dioxide.
10. The utility model provides a system for nitrogen gas and carbon dioxide are prepared in step to oil field boiler flue gas which characterized in that includes: the system comprises a water washing tower (1), a circulating pump (2), a cooler (3), a flue gas compressor (4), a dryer (5), a carbon-nitrogen separation PSA (6), a PSA compressor (7), a carbon dioxide purification PSA (8), a nitrogen purification PSA (9), a rectification compressor (10), a precooler (11), a rectification tower (12) and a liquid carbon dioxide storage tank (13);
the inlet at the bottom of the water washing tower (1) is flue gas to be treated, the inlet at the upper part of the water washing tower (1) is connected with the outlet of the cooler (3), the outlet at the bottom of the water washing tower (1) is connected with the inlet of the circulating pump (2), and the outlet at the upper part of the water washing tower (1) is connected with the inlet of the flue gas compressor (4);
the outlet of the circulating pump (2) is connected with the inlet of the cooler (3);
the inlet of the dryer (5) is connected with the outlet of the flue gas compressor (4);
the inlet of the carbon-nitrogen separation PSA (6) is connected with the outlet of the dryer (5), the lower outlet of the carbon-nitrogen separation PSA (6) is connected with a PSA compressor (7), the upper outlet of the carbon-nitrogen separation PSA (6) is mixed with the upper outlet of the carbon dioxide purification PSA (8) and then is connected with the inlet of a nitrogen purification PSA (9);
the outlet of the PSA compressor (7) is connected with the inlet of the carbon dioxide purification PSA (8);
the inlet of the rectification compressor (10) is connected with the lower outlet of the carbon dioxide purification PSA (8), and the outlet of the rectification compressor (10) is connected with the first inlet of the precooler (11);
a first outlet of the precooler (11) is connected with an inlet of the rectifying tower (12), and a second outlet of the rectifying compressor (10) is precooled and recycled low-concentration carbon dioxide; the second inlet of the rectification compressor (10) is connected with the outlet at the upper part of the rectification tower (12);
an outlet at the upper part of the rectifying tower (12) is connected with an inlet of the liquid carbon dioxide storage tank (13);
the outlet of the liquid carbon dioxide storage tank (13) is product liquid carbon dioxide;
the top outlet of the nitrogen purification PSA (9) is low-concentration nitrogen, and the bottom outlet is product nitrogen.
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| CN202210627996.3A CN114852973A (en) | 2022-06-02 | 2022-06-02 | Method and system for synchronously preparing nitrogen and carbon dioxide from oil field boiler flue gas |
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| CN202210627996.3A CN114852973A (en) | 2022-06-02 | 2022-06-02 | Method and system for synchronously preparing nitrogen and carbon dioxide from oil field boiler flue gas |
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Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20090101868A1 (en) * | 2007-10-22 | 2009-04-23 | Fengshan Zhang | Method for reclaim of carbon dioxide and nitrogen from boiler flue gas |
| CN102141336A (en) * | 2011-03-25 | 2011-08-03 | 东南大学 | Device and method for gathering and liquefying carbon dioxide and generating nitrogen from smoke gas |
| CN113975950A (en) * | 2021-11-04 | 2022-01-28 | 大连理工大学 | System and method for synchronously recovering carbon dioxide and nitrogen in flue gas by chemical method and PSA (pressure swing adsorption) method |
| CN216481836U (en) * | 2021-12-06 | 2022-05-10 | 大连理工大学 | System for boiler flue gas retrieves nitrogen gas and carbon dioxide in step |
| CN217868141U (en) * | 2022-06-02 | 2022-11-22 | 西安本清化学技术有限公司 | System for synchronously preparing nitrogen and carbon dioxide from oil field boiler flue gas |
-
2022
- 2022-06-02 CN CN202210627996.3A patent/CN114852973A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20090101868A1 (en) * | 2007-10-22 | 2009-04-23 | Fengshan Zhang | Method for reclaim of carbon dioxide and nitrogen from boiler flue gas |
| CN102141336A (en) * | 2011-03-25 | 2011-08-03 | 东南大学 | Device and method for gathering and liquefying carbon dioxide and generating nitrogen from smoke gas |
| CN113975950A (en) * | 2021-11-04 | 2022-01-28 | 大连理工大学 | System and method for synchronously recovering carbon dioxide and nitrogen in flue gas by chemical method and PSA (pressure swing adsorption) method |
| CN216481836U (en) * | 2021-12-06 | 2022-05-10 | 大连理工大学 | System for boiler flue gas retrieves nitrogen gas and carbon dioxide in step |
| CN217868141U (en) * | 2022-06-02 | 2022-11-22 | 西安本清化学技术有限公司 | System for synchronously preparing nitrogen and carbon dioxide from oil field boiler flue gas |
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