CN116099333A - Produced gas chemical method carbon capture system - Google Patents
Produced gas chemical method carbon capture system Download PDFInfo
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- CN116099333A CN116099333A CN202310390608.9A CN202310390608A CN116099333A CN 116099333 A CN116099333 A CN 116099333A CN 202310390608 A CN202310390608 A CN 202310390608A CN 116099333 A CN116099333 A CN 116099333A
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- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 title claims abstract description 22
- 229910052799 carbon Inorganic materials 0.000 title claims abstract description 22
- 238000000034 method Methods 0.000 title claims abstract description 22
- 239000000126 substance Substances 0.000 title claims abstract description 9
- 239000007789 gas Substances 0.000 claims abstract description 188
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 134
- 238000010521 absorption reaction Methods 0.000 claims abstract description 129
- 239000007788 liquid Substances 0.000 claims abstract description 129
- 239000003546 flue gas Substances 0.000 claims abstract description 95
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 91
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 67
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 67
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 92
- 238000005406 washing Methods 0.000 claims description 54
- 238000011069 regeneration method Methods 0.000 claims description 35
- 230000008929 regeneration Effects 0.000 claims description 34
- 229920006395 saturated elastomer Polymers 0.000 claims description 10
- 238000001311 chemical methods and process Methods 0.000 claims description 9
- 238000001816 cooling Methods 0.000 claims description 9
- 238000005262 decarbonization Methods 0.000 claims description 7
- 238000000605 extraction Methods 0.000 claims description 7
- 238000006243 chemical reaction Methods 0.000 claims description 3
- 239000000779 smoke Substances 0.000 claims description 3
- 239000006096 absorbing agent Substances 0.000 claims 2
- 238000003860 storage Methods 0.000 description 12
- 238000010586 diagram Methods 0.000 description 4
- 230000005611 electricity Effects 0.000 description 4
- 238000011084 recovery Methods 0.000 description 4
- 238000010438 heat treatment Methods 0.000 description 3
- 238000005261 decarburization Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 210000002268 wool Anatomy 0.000 description 2
- 150000001335 aliphatic alkanes Chemical class 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
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- E—FIXED CONSTRUCTIONS
- E21—EARTH OR ROCK DRILLING; MINING
- E21B—EARTH OR ROCK DRILLING; OBTAINING OIL, GAS, WATER, SOLUBLE OR MELTABLE MATERIALS OR A SLURRY OF MINERALS FROM WELLS
- E21B43/00—Methods or apparatus for obtaining oil, gas, water, soluble or meltable materials or a slurry of minerals from wells
- E21B43/16—Enhanced recovery methods for obtaining hydrocarbons
- E21B43/164—Injecting CO2 or carbonated water
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1425—Regeneration of liquid absorbents
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
- B01D53/1462—Removing mixtures of hydrogen sulfide and carbon dioxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
- B01D53/1481—Removing sulfur dioxide or sulfur trioxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
- F23G7/06—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/40—Nitrogen compounds
-
- 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
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Analytical Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Environmental & Geological Engineering (AREA)
- Geology (AREA)
- Mining & Mineral Resources (AREA)
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- General Life Sciences & Earth Sciences (AREA)
- Geochemistry & Mineralogy (AREA)
- Physics & Mathematics (AREA)
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- General Engineering & Computer Science (AREA)
- Gas Separation By Absorption (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention relates to the technical field of produced gas treatment, and provides a produced gas chemical method carbon capture system. The concentration of carbon dioxide in the flue gas is low, the partial pressure is low, the lean solution of the absorption liquid firstly enters the flue gas absorption tower to remove the carbon dioxide in the flue gas, and the semi-rich solution of the absorption liquid then enters the produced gas absorption tower.
Description
Technical Field
The invention relates to the technical field of produced gas treatment, in particular to a produced gas chemical method carbon capture system.
Background
After the oil field is displaced by carbon dioxide, the produced gas often escapes. The produced gas has high pressure (0.2-1.0 Mpa) and CO 2 High concentration (15-70 vol%) and 25-45% of heat value gas (C1-C4 alkane). The treatment methods of the produced gas generally include an absorption/adsorption method, a membrane separation method and the like, and the chemical absorption method is adopted for the produced gas trapping system at present to trap carbon dioxide in consideration of factors such as carbon dioxide trapping cost, technical maturity and the likeBefore, often need to wash raw materials gas in the washing tower, control temperature, however current entrapment system can't retrieve carbon dioxide is whole, and often needs outside steam heat supply, brings very big processing cost for the enterprise, is unfavorable for popularization and application.
Disclosure of Invention
The invention aims to provide a carbon capture system for a chemical method of produced gas, wherein the produced gas after decarbonization is used for the regeneration process of absorption liquid by generating steam through a steam boiler, and the generated high-temperature flue gas enters a flue gas absorption unit to remove carbon dioxide in the flue gas, so that the carbon dioxide capture process of the produced gas in a full flow and full flow way is realized. The concentration of carbon dioxide in the flue gas is low, the partial pressure is low, the lean solution of the absorption liquid firstly enters the flue gas absorption tower to remove the carbon dioxide in the flue gas, and the semi-rich solution of the absorption liquid then enters the produced gas absorption tower. And regulating the flow of lean liquid entering the flue gas absorption tower according to the decarburization efficiency of the flue gas and the produced gas absorption tower.
The high-temperature flue gas heats the produced gas in the pretreatment process, so that the reaction rate and the decarburization efficiency of the produced gas absorption tower are improved. (the heat exchange unit consists of a heater, a cooler, a water storage tank and a water pump, circulating water in the water storage tank is sent into the cooler in the produced gas absorption unit by the water pump to be cooled to 30-50 ℃, and the cooled circulating water is fused into the heater in the flue gas absorption unit to be heated to 50-70 ℃ and is sent back to the water storage tank).
The produced gas after decarbonization enters a steam boiler, and wet saturated steam recovers the heat of the flue gas through a steam superheater to reach a superheated state. The superheated steam enters a reboiler for the absorption liquid regeneration process, and the steam condensate water is further cooled by a rich liquid heater and is sent back to a boiler water tank.
Specifically, the embodiment of the invention is realized by the following technical scheme:
(1) The device consists of a produced gas carbon dioxide absorption unit, a produced gas boiler unit, a flue gas carbon dioxide absorption unit and an absorption liquid regeneration unit.
Wherein the produced gas enters a produced gas carbon dioxide absorption unit to remove SO in the produced gas x 、NO x And H 2 S and carbon dioxide isogasA body; the decarbonized produced gas enters a produced gas boiler unit to be combusted to generate steam and smoke; the flue gas generated by the gas extraction boiler unit is sent to a flue gas carbon dioxide absorption unit to remove SO in the flue gas x 、NO x And gases such as carbon dioxide; and sending the rich liquid of the absorption liquid generated by the produced gas carbon dioxide absorption unit and the flue gas carbon dioxide absorption unit into an absorption liquid regeneration unit to regenerate high-purity carbon dioxide gas.
Further, the produced gas carbon dioxide absorbing unit comprises a produced gas pretreatment tower, a circulating pump, a washing water heater, a produced gas absorbing tower, a circulating water booster pump, a circulating water tank, a semi-rich liquid pump, a water washing water storage tank, a water washing cooler, a water washing pump and a rich liquid pump,
the produced gas enters from the lower part of the produced gas pretreatment tower; heating the washing liquid by a circulating pump through a washing water heater, and feeding the washing liquid into an absorption tower from the top of the produced gas pretreatment tower; countercurrent heat and mass transfer of washing water and produced gas, and removal of SOx, NOx and H in the produced gas 2 S and other gases; meanwhile, the washing water is heated to 30-50 ℃ after heating.
The pretreated produced gas reaches a water-wet saturated state, enters from the bottom of the produced gas absorption tower, and carries out countercurrent mass transfer and heat transfer with the semi-rich liquid of the absorption liquid from the flue gas carbon dioxide absorption unit, and the rich liquid of the absorption liquid flows out from the bottom of the produced gas absorption tower. And (3) after decarbonization, the produced gas enters a tail gas washing section of a produced gas absorption tower to be washed and cooled, and meanwhile, absorption liquid carried in the produced gas is removed and sent into a steam boiler.
Further, the produced gas boiler unit comprises a steam boiler, a steam superheater, a boiler water tank and a boiler water pump;
the decarbonized produced gas enters a steam boiler to burn to generate saturated steam of 0.3-0.7Mpa, enters a steam superheater, is heated to a superheated state by high-temperature flue gas, and is sent into a reboiler of an absorption liquid regeneration unit for the absorption liquid regeneration process. The condensed water at the outlet of the reboiler returns to the boiler water tank and is pumped into the steam boiler by the boiler water pump.
Further, the flue gas carbon dioxide absorption unit comprises a flue gas pretreatment tower, a flue gas absorption tower, a water pump, a cooler, a flue gas rich liquid pump, a flue gas tail gas washing cooler, a tail gas washing water tank and a tail gas washing water pump; the high-temperature flue gas exhausted by the gas extraction boiler unit enters from the bottom of the flue gas pretreatment tower; the washing liquid is cooled by a circulating pump and is sent into a flue gas absorption tower from the upper part of the flue gas pretreatment tower; countercurrent heat and mass transfer is carried out on the washing water and the flue gas, so that gases such as SOx, NOx and the like in the flue gas are removed; meanwhile, the hot washing liquid at the bottom of the flue gas pretreatment tower exchanges heat with a heater in the produced gas carbon dioxide absorption unit through a cooler (the heat exchange unit consists of the heater, the cooler, a water storage tank and a water pump), circulating water in the water storage tank is sent into the cooler in the produced gas absorption unit by the water pump to be cooled to 30-50 ℃, the cooled circulating water is fused into the heater in the flue gas absorption unit to be heated to 50-70 ℃ and is sent back to the water storage tank), and the cooled washing water cools the flue gas to 30-50 ℃.
The pretreated flue gas reaches a water-wet saturated state, enters from the bottom of an absorption tower in a flue gas absorption unit, and is in countercurrent mass transfer and heat transfer with lean liquid of an absorption liquid at the upper part, and semi-rich liquid of the absorption liquid flows out from the bottom of a carbon dioxide absorption tower in a flue gas carbon dioxide absorption unit and is sent into an extraction gas carbon dioxide absorption tower in an extraction gas carbon dioxide absorption unit. And (3) after decarbonization, the flue gas enters an absorption tower tail gas washing section for washing and cooling, and meanwhile absorption liquid carried in the produced gas is removed and discharged into the atmosphere.
Further, the absorption liquid regeneration unit comprises a lean liquid pump, a lean and rich liquid heat exchanger, a lean liquid cooler, a regeneration tower, a rich liquid reheater, a regenerated gas cooler, a gas-liquid separator, a condensate pump and a reboiler;
cold rich liquid at the bottom of an produced gas absorption tower in the produced gas carbon dioxide absorption unit is pumped into a lean rich liquid heat exchanger by a rich liquid pump, hot lean liquid at the bottom of a regeneration tower is pumped into a lean rich liquid heat exchanger by a lean liquid pump, and the cold rich liquid and the hot lean liquid are subjected to heat transfer by the lean rich liquid heat exchanger; and (3) enabling hot rich liquid at the outlet of the lean-rich liquid heat exchanger to enter a rich liquid reheater, recovering heat of steam condensate water at the outlet of the reboiler, and sending the cooled steam condensate water into a water tank of an extracted gas boiler, wherein the hot rich liquid is sent into the upper part of a regeneration tower.
The regenerated gas in the regeneration tower enters a regenerated gas cooler for cooling, and is sent into a regenerated gas-liquid separator, condensed water is pumped back to the upper part of the regeneration tower through a condensed water pump, and the regenerated gas is recoveredHeat quantity; CO 2 The product gas is discharged through the upper part of the gas-liquid separator.
The technical scheme of the embodiment of the invention has at least the following advantages and beneficial effects:
the invention creatively adopts a double-tower process to treat the produced gas, remove carbon dioxide in the produced gas, realize the full-flow and full-flow carbon dioxide capturing process of the produced gas, and basically realize the full recovery of carbon in the produced gas without external steam for heat supply, and the recovery rate of carbon in the produced gas (calculated by carbon dioxide) is more than 90%; and the resources can be recycled, so that the energy consumption is reduced, and one ton of carbon dioxide is recovered: the electricity cost is about 48 yuan (the electricity price is measured by 6 wool one degree), and the water consumption is 3-6 yuan, so that the production and treatment cost of enterprises is greatly reduced.
Drawings
In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings that are needed in the embodiments will be briefly described below, it being understood that the following drawings only illustrate some embodiments of the present invention and therefore should not be considered as limiting the scope, and other related drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.
FIG. 1 is a schematic diagram of a produced gas chemical process carbon capture system provided in an embodiment of the present invention;
FIG. 2 is a schematic diagram of the produced gas carbon dioxide absorption unit of FIG. 1;
FIG. 3 is a schematic view of the produced gas boiler unit of FIG. 1;
FIG. 4 is a schematic diagram of the flue gas carbon dioxide absorption unit of FIG. 1;
FIG. 5 is a schematic diagram of the absorption liquid regeneration unit of FIG. 1;
icon: the system comprises a 1-produced gas carbon dioxide absorption unit, a 2-produced gas boiler unit, a 3-flue gas carbon dioxide absorption unit, a 4-absorption liquid regeneration unit, a 01-produced gas pretreatment tower, a 02-circulating pump, a 03-washing water heater, a 04-circulating water booster pump, a 05-semi-rich liquid pump, a 06-water washing water storage tank, a 07-water washing water cooler, a 08-water washing water pump, a 09-produced gas absorption tower, a 10-rich liquid pump, a 11-lean liquid pump, a 12-lean rich liquid heat exchanger, a 13-lean liquid cooler, a 14-regeneration tower, a 15-rich liquid reheater, a 16-regenerated gas cooler, a 17-gas-liquid separator, a 18-condensate pump, a 19-reboiler, a 20-boiler water tank, a 21-boiler water pump, a 22-steam boiler, a 23-steam superheater, a 24-flue gas absorption tower, a 25-flue gas rich liquid pump, a 26-circulating water tank, a 27-water pump, a 28-flue gas pretreatment tower, a 29-cooler, a 30-tail gas scrubber, a 31-tail gas washing water tank, and a 32-tail gas washing water pump.
Detailed Description
In order to make the objects, technical solutions and advantages of the embodiments of the present invention more clear, the technical solutions of the embodiments of the present invention will be clearly and completely described below. The specific conditions are not noted in the examples and are carried out according to conventional conditions or conditions recommended by the manufacturer. The reagents or apparatus used were conventional products commercially available without the manufacturer's attention.
Example 1
The produced gas full-flow chemical method carbon capture system comprises a produced gas carbon dioxide absorption unit 1, a produced gas boiler unit 2, a flue gas carbon dioxide absorption unit 3 and an absorption liquid regeneration unit 4;
wherein the produced gas enters a produced gas carbon dioxide absorption unit 1 to remove SOx, NOx and H in the produced gas 2 S, gases such as carbon dioxide and the like; the decarbonized produced gas enters a produced gas boiler unit 2 to be combusted to generate steam and smoke; the flue gas generated by the gas extraction boiler unit 2 is sent to the flue gas carbon dioxide absorption unit 3 to remove SOx, NOx, carbon dioxide and other gases in the flue gas; the rich liquid of the absorption liquid generated by the produced gas carbon dioxide absorption unit 1 and the flue gas carbon dioxide absorption unit 3 is sent to the absorption liquid regeneration unit 4 to regenerate high-purity carbon dioxide gas.
In the embodiment, the produced gas carbon dioxide absorbing unit 1 comprises a produced gas pretreatment tower 01, a circulating pump 02, a washing water heater 03, a produced gas absorbing tower 09, a circulating water booster pump 04, a circulating water tank 26, a semi-rich liquid pump 05, a washing water storage tank 06, a washing water cooler 07, a washing water pump 08 and a rich liquid pump 10,
the produced gas enters from the lower part of the produced gas pretreatment tower 01; the washing liquid is sent into the washing water to heat by a circulating pump 02Heating the device 03, and feeding the produced gas into a produced gas absorption tower 09 from the top of the produced gas pretreatment tower 01; countercurrent heat and mass transfer of washing water and produced gas, and removal of SOx, NOx and H in the produced gas 2 S and other gases; meanwhile, the washing water is heated to 30-50 ℃ after heating.
The pretreated produced gas reaches a water-wet saturated state, enters from the bottom of the produced gas absorption tower 09, and carries out countercurrent mass transfer and heat transfer with the semi-rich liquid of the absorption liquid from the flue gas carbon dioxide absorption unit 3, and the rich liquid of the absorption liquid flows out from the bottom of the produced gas absorption tower 09. The decarbonized produced gas enters a tail gas washing section of the produced gas absorption tower 09 for washing and cooling, and meanwhile, absorption liquid carried in the produced gas is removed and sent to a steam boiler 22.
In the present embodiment, the produced gas boiler unit 2 includes a steam boiler 22, a steam superheater 23, a boiler water tank 20, and a boiler water pump 21;
the decarbonized produced gas enters a steam boiler 22 to be combusted to generate saturated steam with the pressure of 0.3-0.7Mpa, enters a steam superheater 23, is heated to a superheated state by high-temperature flue gas, and is sent into a reboiler 19 of an absorption liquid regeneration unit 4 for the absorption liquid regeneration process; the condensed water at the outlet of the reboiler 19 is returned to the boiler water tank 20, and is sent to the steam boiler 22 by the boiler water pump 21.
In this embodiment, the flue gas carbon dioxide absorbing unit 3 includes a flue gas pretreatment tower 28, a flue gas absorbing tower 24, a water pump 27, a cooler 29, a flue gas rich liquid pump 25, a flue gas tail gas washing cooler 30, a tail gas washing water tank 31, and a tail gas washing water pump 32; the high-temperature flue gas exhausted by the produced gas boiler unit 2 enters from the bottom of the flue gas pretreatment tower 28; the washing liquid is sent into a washing water cooler 29 for cooling through a circulating pump 02, and is sent into a flue gas absorption tower 24 from the upper part of a flue gas pretreatment tower 28; countercurrent heat and mass transfer is carried out on the washing water and the flue gas, so that gases such as SOx, NOx and the like in the flue gas are removed; meanwhile, the hot washing liquid at the bottom of the flue gas pretreatment tower 28 exchanges heat with a heater through a cooler 29 (a heat exchange unit consists of the heater, the cooler 29, a water storage tank and a water pump 27), circulating water in the water storage tank is sent into the cooler 29 in the produced gas absorption unit by the water pump 27 to be cooled to 30-50 ℃, the cooled circulating water is fused into the heater in the flue gas absorption unit to be heated to 50-70 ℃ and is sent back to the water storage tank), and the cooled washing water cools the flue gas to 30-50 ℃.
The pretreated flue gas reaches a water-wet saturated state, enters from the bottom of a flue gas absorption tower 24 in a flue gas carbon dioxide absorption unit 3, carries out countercurrent mass transfer and heat transfer with lean liquid of an absorption liquid at the upper part, and semi-rich liquid of the absorption liquid flows out from the bottom of the flue gas absorption tower 24 in the flue gas carbon dioxide absorption unit 3 and is sent into an produced gas absorption tower 09 in a produced gas carbon dioxide absorption unit 1. And after decarbonization, the flue gas enters a tail gas washing section of a flue gas absorption tower 24 for washing and cooling, and meanwhile, absorption liquid carried in produced gas is removed and discharged into the atmosphere.
In the present embodiment, the absorption liquid regeneration unit 4 includes a lean liquid pump 11, a lean-rich liquid heat exchanger 12, a lean liquid cooler 13, a regeneration tower 14, a rich liquid reheater 15, a regeneration gas cooler 16, a gas-liquid separator 17, a condensate pump 18, and a reboiler 19;
the cold rich liquid at the bottom of the produced gas absorption tower 09 in the produced gas carbon dioxide absorption unit 1 is sent into the lean rich liquid heat exchanger 12 by the rich liquid pump 10, the hot lean liquid at the bottom of the regeneration tower 14 is sent into the lean rich liquid heat exchanger 12 by the lean liquid pump 11, and the cold rich liquid and the hot lean liquid are subjected to heat transfer by the lean rich liquid heat exchanger 12; the hot rich liquid at the outlet of the lean-rich liquid heat exchanger 12 enters the rich liquid reheater 15, the heat of steam condensate water at the outlet of the reboiler 19 is recovered, the cooled steam condensate water is sent to the water tank 20 of the produced gas boiler, and the hot rich liquid is sent to the upper part of the regeneration tower 14.
The regenerated gas in the regeneration tower 14 enters a regenerated gas cooler 16 for cooling, is sent into a regenerated gas-liquid separator 17, condensed water is sent back to the upper part of the regeneration tower 14 through a condensate pump 18, and the heat of the regenerated gas is recovered; CO 2 The product gas is discharged through the upper part of the gas-liquid separator 17.
The invention creatively adopts a double-tower process to treat the produced gas, remove the carbon dioxide and other gases in the produced gas, realize the full-flow and full-flow carbon trapping process of the produced gas, and basically can realize the full recovery of carbon in the produced gas without external steam for heat supply, and the treatment process of the embodiment can realize the recovery rate of carbon in the produced gas of more than 90 percent (calculated by carbon dioxide); and the resources can be recycled, so that the energy consumption is reduced, and one ton of carbon dioxide is recovered: the electricity cost is about 48 yuan (the electricity price is measured by 6 wool one degree), and the water consumption is 3-6 yuan, so that the production and treatment cost of enterprises is greatly reduced.
The above is only a preferred embodiment of the present invention, and is not intended to limit the present invention, but various modifications and variations can be made to the present invention by those skilled in the art. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (10)
1. The produced gas chemical method carbon capture system is characterized in that: comprises an extracted gas carbon dioxide absorption unit, an extracted gas boiler unit, a flue gas carbon dioxide absorption unit and an absorption liquid regeneration unit;
the produced gas carbon dioxide absorption unit is used for removing carbon dioxide and other harmful gases in the produced gas; the produced gas after decarbonization enters a produced gas boiler unit to be combusted to produce steam and smoke,
the flue gas generated by the gas extraction boiler unit is sent to a flue gas carbon dioxide absorption unit to remove carbon dioxide and other harmful gases in the flue gas;
and sending the rich liquid of the absorption liquid generated by the produced gas carbon dioxide absorption unit and the flue gas carbon dioxide absorption unit into an absorption liquid regeneration unit to regenerate high-purity carbon dioxide gas.
2. The produced gas chemical process carbon capture system of claim 1, wherein the produced gas carbon dioxide absorption unit comprises a produced gas pretreatment column and a produced gas absorption column; the produced gas enters the produced gas pretreatment tower from the lower part of the produced gas pretreatment tower, is subjected to washing and decarbonization by a washing liquid in the produced gas pretreatment tower, and enters the produced gas absorption tower from the top of the produced gas pretreatment tower.
3. The produced gas chemical method carbon capture system according to claim 2, wherein the pretreated produced gas and the semi-rich liquid of the absorption liquid discharged from the flue gas carbon dioxide absorption unit are subjected to countercurrent mass transfer and heat transfer in the produced gas absorption tower; after the reaction, the rich liquid of the absorption liquid is sent to an absorption liquid regeneration unit from the bottom of the produced gas absorption tower.
4. The produced gas chemical process carbon capture system according to claim 2, wherein the produced gas is decarbonized by the produced gas pretreatment tower, enters the produced gas absorption tower for washing and cooling, and simultaneously removes absorption liquid entrained in the produced gas, and then is sent to the produced gas boiler unit.
5. The produced gas chemical process carbon capture system of any one of claims 1-4, wherein the produced gas boiler unit comprises a steam boiler, a steam superheater, and a boiler water tank; the decarbonized produced gas enters a steam boiler to be combusted to generate saturated steam, the saturated steam enters a steam superheater, and the saturated steam is sent to an absorption liquid regeneration unit after being heated to an overheat state by high-temperature flue gas.
6. The produced gas chemical process carbon capture system of claim 5, wherein the flue gas carbon dioxide absorption unit comprises: a flue gas pretreatment tower and a flue gas absorption tower;
the high-temperature flue gas discharged by the steam superheater of the gas extraction boiler unit enters from the bottom of the flue gas pretreatment tower, is washed and cooled by cooling washing liquid entering from the upper part in the flue gas pretreatment tower, and is discharged from the top of the flue gas pretreatment tower to enter the flue gas absorption tower.
7. The produced gas chemical process carbon capture system of claim 6, further comprising a cooler in communication with the flue gas pretreatment column, a feedwater heater in communication with the produced gas pretreatment column, and a circulating water tank located between the cooler and the feedwater heater;
and the washing liquid of the flue gas pretreatment tower and the washing liquid of the produced gas pretreatment tower exchange heat through a cooler, a circulating water tank and a washing water heater and are recycled.
8. The produced gas chemical process carbon capture system of claim 7, wherein the pretreated flue gas enters from the bottom of the flue gas absorber column and is counter-currently mass and heat transferred with the upper absorber liquid lean liquid; after the reaction, the semi-rich liquid of the absorption liquid flows out from the bottom of the flue gas absorption tower and is sent into the produced gas absorption tower.
9. The produced gas chemical process carbon capture system according to claim 8, wherein the decarbonized flue gas enters a flue gas absorption tower for washing and cooling, and meanwhile, absorption liquid carried in the flue gas is removed and discharged into the atmosphere.
10. The produced gas chemical process carbon capture system of claim 1, wherein the absorption liquid regeneration unit comprises: a regeneration tower, a gas-liquid separator and a reboiler; superheated steam produced by the steam superheater enters a reboiler and then is sent into a regeneration tower, rich liquid and lean liquid are sent into the regeneration tower after heat exchange, and regenerated gas in the regeneration tower is cooled and separated and then discharged into CO 2 Product gas.
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Citations (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20110127218A1 (en) * | 2008-02-18 | 2011-06-02 | Fluor Technologies Corporation | Regenerator Configurations and Methods with Reduced Steam Demand |
| CN102442667A (en) * | 2011-09-30 | 2012-05-09 | 白洪亮 | Catching and refining device of carbon dioxide gas |
| WO2013061761A1 (en) * | 2011-10-28 | 2013-05-02 | 株式会社Ihi | Carbon dioxide recovery method and recovery device |
| US20130174566A1 (en) * | 2010-09-28 | 2013-07-11 | Roland Birley | Method for removing carbon dioxide, and also gas turbine installation with carbon dioxide removal |
| US20130341924A1 (en) * | 2011-08-08 | 2013-12-26 | Michael J. Lewis | Process for enhanced oil recovery using capture of carbon dioxide |
| US20140041523A1 (en) * | 2012-08-09 | 2014-02-13 | Mitsubishi Heavy Industries, Ltd. | Exhaust gas treatment system |
| JP2014091091A (en) * | 2012-11-05 | 2014-05-19 | Babcock-Hitachi Co Ltd | Device and method for absorbing carbon dioxide |
| CN112619370A (en) * | 2020-12-01 | 2021-04-09 | 成都正升能源技术开发有限公司 | Carbon dioxide flooding oilfield associated gas recovery device and use method thereof |
| CN114950117A (en) * | 2022-01-20 | 2022-08-30 | 中国中煤能源集团有限公司 | Industrial carbon sequestration system and method for absorbing carbon dioxide gas |
| CN115463516A (en) * | 2022-07-22 | 2022-12-13 | 国家能源集团新能源技术研究院有限公司 | System and method for using flue gas waste heat for carbon capture regeneration |
| US20220410062A1 (en) * | 2019-12-27 | 2022-12-29 | Mitsubishi Heavy Industries, Ltd. | Boiler plant and carbon dioxide removal method |
-
2023
- 2023-04-13 CN CN202310390608.9A patent/CN116099333B/en active Active
Patent Citations (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20110127218A1 (en) * | 2008-02-18 | 2011-06-02 | Fluor Technologies Corporation | Regenerator Configurations and Methods with Reduced Steam Demand |
| US20130174566A1 (en) * | 2010-09-28 | 2013-07-11 | Roland Birley | Method for removing carbon dioxide, and also gas turbine installation with carbon dioxide removal |
| US20130341924A1 (en) * | 2011-08-08 | 2013-12-26 | Michael J. Lewis | Process for enhanced oil recovery using capture of carbon dioxide |
| CN102442667A (en) * | 2011-09-30 | 2012-05-09 | 白洪亮 | Catching and refining device of carbon dioxide gas |
| WO2013061761A1 (en) * | 2011-10-28 | 2013-05-02 | 株式会社Ihi | Carbon dioxide recovery method and recovery device |
| US20140041523A1 (en) * | 2012-08-09 | 2014-02-13 | Mitsubishi Heavy Industries, Ltd. | Exhaust gas treatment system |
| JP2014091091A (en) * | 2012-11-05 | 2014-05-19 | Babcock-Hitachi Co Ltd | Device and method for absorbing carbon dioxide |
| US20220410062A1 (en) * | 2019-12-27 | 2022-12-29 | Mitsubishi Heavy Industries, Ltd. | Boiler plant and carbon dioxide removal method |
| CN112619370A (en) * | 2020-12-01 | 2021-04-09 | 成都正升能源技术开发有限公司 | Carbon dioxide flooding oilfield associated gas recovery device and use method thereof |
| CN114950117A (en) * | 2022-01-20 | 2022-08-30 | 中国中煤能源集团有限公司 | Industrial carbon sequestration system and method for absorbing carbon dioxide gas |
| CN115463516A (en) * | 2022-07-22 | 2022-12-13 | 国家能源集团新能源技术研究院有限公司 | System and method for using flue gas waste heat for carbon capture regeneration |
Non-Patent Citations (2)
| Title |
|---|
| 周德彪: "EOR采出气CO2分离工艺模拟研究", 《中国优秀硕士学位论文全文数据库 工程科技I辑》, no. 4, pages 1 - 92 * |
| 马鹏飞，韩波: "油田CO2驱产出气处置方案及 CO2捕集回注工艺", 《化工进展》, vol. 36, no. 1, pages 533 - 539 * |
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