CN114191942A - Flue gas CO2Hypergravity regeneration energy-saving process for trapping system - Google Patents
Flue gas CO2Hypergravity regeneration energy-saving process for trapping system Download PDFInfo
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- CN114191942A CN114191942A CN202111142948.7A CN202111142948A CN114191942A CN 114191942 A CN114191942 A CN 114191942A CN 202111142948 A CN202111142948 A CN 202111142948A CN 114191942 A CN114191942 A CN 114191942A
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- 238000000034 method Methods 0.000 title claims abstract description 61
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 55
- 239000003546 flue gas Substances 0.000 title claims abstract description 55
- 238000011069 regeneration method Methods 0.000 title claims abstract description 55
- 230000008929 regeneration Effects 0.000 title claims abstract description 54
- 230000008569 process Effects 0.000 title claims abstract description 53
- 239000007788 liquid Substances 0.000 claims abstract description 106
- 238000010521 absorption reaction Methods 0.000 claims abstract description 80
- 238000009835 boiling Methods 0.000 claims abstract description 66
- 230000002745 absorbent Effects 0.000 claims abstract description 31
- 239000002250 absorbent Substances 0.000 claims abstract description 31
- 238000001816 cooling Methods 0.000 claims abstract description 30
- 238000003795 desorption Methods 0.000 claims abstract description 28
- 230000001360 synchronised effect Effects 0.000 claims abstract description 8
- 239000007789 gas Substances 0.000 claims description 70
- 230000001105 regulatory effect Effects 0.000 claims description 29
- 238000010438 heat treatment Methods 0.000 claims description 21
- 239000012071 phase Substances 0.000 claims description 19
- 238000000926 separation method Methods 0.000 claims description 16
- 238000006243 chemical reaction Methods 0.000 claims description 11
- 238000000746 purification Methods 0.000 claims description 9
- 238000001514 detection method Methods 0.000 claims description 8
- 230000009471 action Effects 0.000 claims description 7
- 230000001276 controlling effect Effects 0.000 claims description 7
- 238000006477 desulfuration reaction Methods 0.000 claims description 7
- 230000023556 desulfurization Effects 0.000 claims description 7
- 239000000428 dust Substances 0.000 claims description 7
- 239000007791 liquid phase Substances 0.000 claims description 7
- 238000002156 mixing Methods 0.000 claims description 7
- 239000000203 mixture Substances 0.000 claims description 7
- 238000012805 post-processing Methods 0.000 claims description 7
- 238000005507 spraying Methods 0.000 claims description 7
- 238000012546 transfer Methods 0.000 claims description 7
- 238000005728 strengthening Methods 0.000 claims description 6
- 238000005485 electric heating Methods 0.000 claims description 5
- 238000007599 discharging Methods 0.000 claims description 2
- 239000000126 substance Substances 0.000 abstract description 13
- 238000004064 recycling Methods 0.000 abstract description 10
- 239000003814 drug Substances 0.000 abstract description 6
- 230000015556 catabolic process Effects 0.000 abstract description 3
- 238000006731 degradation reaction Methods 0.000 abstract description 3
- 230000006866 deterioration Effects 0.000 abstract description 3
- 238000003912 environmental pollution Methods 0.000 abstract description 3
- 230000007613 environmental effect Effects 0.000 abstract description 2
- 229910002092 carbon dioxide Inorganic materials 0.000 description 31
- 238000005265 energy consumption Methods 0.000 description 5
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 230000000694 effects Effects 0.000 description 3
- 150000001412 amines Chemical class 0.000 description 2
- 239000002803 fossil fuel Substances 0.000 description 2
- 239000010865 sewage Substances 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 238000011156 evaluation Methods 0.000 description 1
- 239000005431 greenhouse gas Substances 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000009919 sequestration Effects 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 230000004083 survival effect Effects 0.000 description 1
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- 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
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- 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
- B01D53/1475—Removing carbon dioxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
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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
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
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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
- 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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- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention is suitable for the field of environmental protection, and provides a supergravity regeneration energy-saving process of a flue gas CO2 trapping system, which comprises the following steps: absorption of CO2, heat exchange, desorption of CO2, cooling, synchronous operation and aftertreatment; the flue gas CO2 trapping system adopting the chemical absorption method adopts a coupled regeneration process of the hypergravity reactor, the solution boiler and the boiling liquid separator, so that the medicament loss and the degradation and deterioration of the medicament are reduced, the recycling times of the chemical absorbent are improved, the characteristics of low consumption, low emission and high efficiency of recycling economy are met, and the purposes of recycling and reducing environmental pollution are achieved.
Description
Technical Field
The invention belongs to the field of environmental protection, and particularly relates to flue gas CO2The capture system hypergravity regeneration energy-saving process.
Background
In recent years, the atmospheric environment continues to deteriorate due to the combustion of fossil fuels, and the "greenhouse effect" caused thereby is becoming more and more serious to threaten human survival. CO22Not only are major contributors to greenhouse gases, their hazards last longer. To alleviate the effect of "greenhouse effect", the first solution to CO should be2The emission reduction and the recycling are realized.
The carbon capture and sequestration technology isReduction of CO emissions into the atmosphere with reduced current fossil fuel usage2The most direct and efficient way of gas volume.
The method for separating carbon dioxide from flue gas by the CCS technology mainly comprises the following steps: membrane separation, physical adsorption, cryogenic distillation, absorption separation, and the like. CO capture by chemical absorption2The method is widely used due to the high absorption rate, high absorption efficiency, simple process and mature technology, and a plurality of demonstration evaluation projects are built at home and abroad. CO capture by chemical absorption2The main disadvantage of the technology is the high energy consumption of the regeneration system, in order to reduce CO2Regeneration energy consumption and CO reduction2Trapping cost, and domestic and foreign scholars are continuously optimizing and developing the existing process to develop new CO2And (4) a trapping regeneration process.
Disclosure of Invention
The embodiment of the invention aims to provide flue gas CO2A hypergravity regeneration energy-saving process of a capture system, aiming at solving the problem of CO capture by the existing chemical absorption method2The technical energy consumption is too high.
The embodiment of the invention is realized by the following steps of providing the flue gas CO2The hypergravity regeneration energy-saving process of the trapping system comprises the following steps:
S1.CO2absorption of (2): carrying out desulfurization, denitrification and dust removal on flue gas discharged by a coal-fired power plant through a deep purification tower; controlling the temperature of the discharged flue gas; the flue gas enters the absorption tower from bottom to top after being pressurized by the induced draft fan, the barren liquor absorbent enters the absorption tower from top to bottom, and the barren liquor absorbent and the absorption tower are in countercurrent contact to finish CO2The absorption process of (2);
s2, heat exchange: the decarbonized flue gas is discharged from a tail gas discharge port at the top of the absorption tower, and CO is absorbed2Discharging a rich solution of the gas from the bottom of the absorption tower, and introducing a cold rich solution pressurized by a rich solution pump into a lean rich solution heat exchanger for heat exchange, wherein the temperature of the cold rich solution after heat exchange is 90-95 ℃;
S3.CO2desorption: spraying the cold rich liquid after heat exchange into a supergravity reactor, and strengthening the relative speed and mutual contact between phases by utilizing the flowing behavior of a multi-phase flow system under the supergravity condition, thereby realizing mass transferHeat transfer process and chemical reaction process to make CO2Rapid desorption from the absorbent;
s4, cooling: the desorbed regeneration gas enters a regeneration gas separator through a regeneration gas outlet to be separated to obtain product gas; the desorbed barren solution is pressurized by a barren solution pump from a barren solution outlet of the supergravity reactor and then enters a barren and rich solution heat exchanger for heat exchange and cooling; cooling the lean solution in a lean solution cooler, feeding the cooled lean solution into an absorption tower, and starting a new absorption process;
s5, synchronous operation: part of the barren solution flows into the siphon type solution boiler through an electric regulating valve on a pipeline branch of the barren solution pump of the supergravity reactor to be heated, and the heated solution and CO desorbed in the heating process2Mixing gas phase and liquid phase, and introducing the mixture into a boiling liquid separator from a boiling liquid outlet under the siphoning action of a solution boiler for gas-liquid separation;
s6, post-processing: the separated desorption gas enters the super-gravity reactor from a gas outlet at the top of the boiling liquid separator, and the separated solution enters the solution boiler through a solution outlet at the bottom of the boiling liquid separator to be continuously circulated;
s7, an electric regulating valve is installed on a pipeline branch line of the barren liquid pump pipeline and interlocked with a liquid level detection system installed on the boiling liquid separator, and when the liquid level of the boiling liquid separator is too high, the opening degree of the electric regulating valve is reduced; when the liquid level of the boiling liquid separator is too low, the opening of the electric regulating valve is increased, so that the stable circulation of the boiling separation system is realized.
According to a further technical scheme, according to S1, the temperature of the flue gas is 35-45 ℃.
According to a further technical scheme, the temperature of the cold pregnant solution is 50-55 ℃ according to S1.
According to a further technical scheme, according to S4, the temperature of heat exchange and cooling of the barren solution is 55-65 ℃.
In a further technical scheme, the temperature of the lean solution after being cooled by a lean solution cooler is 40-45 ℃.
According to a further aspect, the solution boiler may be heated in the form of electrical heating or steam heating according to S5.
According to a further technical scheme, according to S7, the absorbent lean-rich liquid is recycled.
The embodiment of the invention provides flue gas CO2The invention relates to a hypergravity regeneration energy-saving process of a trapping system, which improves the prior organic amine chemical absorption process, adopts a hypergravity machine to replace a conventional desorption tower to heat and regenerate absorption liquid, and can realize the miniaturization, the agility, the skid-mounting and the modularization of a desorption system. Firstly proposes the chemical absorption method for flue gas CO2The trapping system adopts a coupled regeneration process of the hypergravity reactor, the solution boiler and the boiling liquid separator to replace the original regeneration process of the desorption tower and the boiling device, so that the size of equipment is greatly reduced, and the device has the advantages of miniaturization, flexibility, high efficiency, small investment, skid-mounted equipment, modularization and the like, saves the investment cost and obviously reduces the regeneration energy consumption. Chemical absorption method for flue gas CO2The coupled regeneration process of the 'super-gravity reactor, the solution boiler and the boiling liquid separator' of the trapping system reduces the medicament loss and the degradation and deterioration of the medicament, improves the recycling times of the chemical absorbent, meets the characteristics of low consumption, low emission and high efficiency of recycling economy, and achieves the purposes of recycling and reducing environmental pollution.
Drawings
Fig. 1 is a schematic structural diagram of an embodiment of the present invention.
In the drawings: 1 deep purification tower, 2 purification tower pumps, 3 absorption towers, 4 draught fans, 5 tail gas discharge ports, 6 rich liquor pumps, 7 lean liquor coolers, 8 lean liquor heat exchangers, 9 lean liquor pumps, 10 super-gravity reactors, 11 solution boilers, 12 boiling liquor separators, 13 regeneration gas separators, 14 product gas, 15 sewage outlets, 16 rich liquor inlets, 17 regeneration gas outlets, 18 lean liquor outlets, 19 boiling liquor outlets, 20 boiling liquor inlets, 21 liquid level detection systems, 22 electric regulating valves, 23 sewage outlets II, 24 gas outlets and 25 solution outlets.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention is described in further detail below with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are merely illustrative of the invention and are not intended to limit the invention.
Specific implementations of the present invention are described in detail below with reference to specific embodiments.
Example one
As shown in fig. 1, a flue gas CO is provided for one embodiment of the present invention2The hypergravity regeneration energy-saving process of the trapping system comprises the following steps:
S1.CO2absorption of (2): carrying out desulfurization, denitrification and dust removal on flue gas discharged by a coal-fired power plant through a deep purification tower 1; controlling the temperature of the discharged flue gas to be 35 ℃; the flue gas enters the absorption tower 3 from bottom to top after being pressurized by the induced draft fan 4, the barren liquor absorbent enters the absorption tower from top to bottom, and the barren liquor absorbent and the absorption tower are in countercurrent contact to finish CO2The absorption process of (2);
s2, heat exchange: the decarbonized flue gas is discharged from a tail gas discharge port 5 at the top of the absorption tower, and CO is absorbed2The rich solution of the gas is discharged from the bottom of the absorption tower, and the cold rich solution pressurized by the rich solution pump 6 enters the lean rich solution heat exchanger 8 for heat exchange at the temperature of 50 ℃. The temperature of the cold rich liquid after heat exchange is 90 ℃;
S3.CO2desorption: spraying the cold rich liquid after heat exchange into a supergravity reactor 10, and strengthening the relative speed and mutual contact between phases by utilizing the flowing behavior of a multi-phase flow system under the supergravity condition, thereby realizing the mass and heat transfer process and the chemical reaction process, and leading CO to be subjected to the reaction2Rapid desorption from the absorbent;
s4, cooling: the desorbed regeneration gas enters a regeneration gas separator 13 through a regeneration gas outlet 17 and is separated to obtain product gas; the desorbed barren solution is pressurized by a barren solution outlet 18 of the supergravity reactor through a barren solution pump 9 and then enters a barren and rich solution heat exchanger 8 for heat exchange and cooling, wherein the temperature of the heat exchange and cooling of the barren solution is 55 ℃; and cooling the lean solution in a lean solution cooler 7, wherein the temperature of the lean solution cooled by the lean solution cooler 7 is 40 ℃. The cooled barren solution enters an absorption tower 3 and starts a new absorption process;
s5, synchronous operation: part of the lean solution flows into the siphon-type solution boiler 11 for heating through an electric control valve 22 on the pipeline branch of the lean solution pump of the super-gravity reactor, and the solution boiler 11 can be heated in a modeEither electrically or steam heated. Heated solution and CO desorbed during heating2Mixing gas phase and liquid phase, and introducing the mixture into a boiling liquid separator 12 from a boiling liquid outlet 19 for gas-liquid separation under the siphoning action of a solution boiler 11;
s6, post-processing: the separated desorption gas enters the super-gravity reactor 10 from a gas outlet 24 at the top of the boiling liquid separator 12, and the separated solution enters the solution boiler 11 through a solution outlet 25 at the bottom of the boiling liquid separator 12 for continuous circulation;
s7, an electric regulating valve 22 is installed on a pipeline branch pipeline of the barren liquor pump 9, the electric regulating valve 22 is interlocked with a liquid level detection system 21 installed on the boiling liquid separator 12, and when the liquid level of the boiling liquid separator 12 is too high, the opening degree of the electric regulating valve 22 is reduced; when the liquid level of the boiling liquid separator 12 is too low, the opening degree of the electric regulating valve 22 is increased, so that stable circulation of the boiling separation system 12 is realized, and the absorbent lean and rich liquid is recycled.
Example two
As shown in fig. 1, a flue gas CO is provided for one embodiment of the present invention2The hypergravity regeneration energy-saving process of the trapping system comprises the following steps:
S1.CO2absorption of (2): carrying out desulfurization, denitrification and dust removal on flue gas discharged by a coal-fired power plant through a deep purification tower 1; controlling the temperature of the discharged flue gas to be 36 ℃; the flue gas enters the absorption tower 3 from bottom to top after being pressurized by the induced draft fan 4, the barren liquor absorbent enters the absorption tower from top to bottom, and the barren liquor absorbent and the absorption tower are in countercurrent contact to finish CO2The absorption process of (2);
s2, heat exchange: the decarbonized flue gas is discharged from a tail gas discharge port 5 at the top of the absorption tower, and CO is absorbed2The rich solution of the gas is discharged from the bottom of the absorption tower, and the cold rich solution pressurized by the rich solution pump 6 enters the lean rich solution heat exchanger 8 for heat exchange at the temperature of 51 ℃. The temperature of the cold rich liquid after heat exchange is 91 ℃;
S3.CO2desorption: spraying the cold rich liquid after heat exchange into a supergravity reactor 10, and strengthening the relative speed and mutual contact between phases by utilizing the flowing behavior of a multi-phase flow system under the supergravity condition, thereby realizing the mass and heat transfer process and the chemical reaction process, and leading CO to be subjected to the reaction2Rapid desorption from the absorbent;
s4, cooling: the desorbed regeneration gas enters a regeneration gas separator 13 through a regeneration gas outlet 17 and is separated to obtain product gas; the desorbed barren solution is pressurized by a barren solution outlet 18 of the supergravity reactor through a barren solution pump 9 and then enters a barren and rich solution heat exchanger 8 for heat exchange and cooling, wherein the temperature of the heat exchange and cooling of the barren solution is 51 ℃; and cooling the lean solution in a lean solution cooler 7, wherein the temperature of the lean solution cooled by the lean solution cooler 7 is 41 ℃. The cooled barren solution enters an absorption tower 3 and starts a new absorption process;
s5, synchronous operation: part of the lean solution flows into the siphon-type solution boiler 11 via the electric control valve 22 on the branch of the pipeline of the high-gravity reactor lean solution pump for heating, and the solution boiler 11 can be heated by electric heating or steam heating. Heated solution and CO desorbed during heating2Mixing gas phase and liquid phase, and introducing the mixture into a boiling liquid separator 12 from a boiling liquid outlet 19 for gas-liquid separation under the siphoning action of a solution boiler 11;
s6, post-processing: the separated desorption gas enters the super-gravity reactor 10 from a gas outlet 24 at the top of the boiling liquid separator 12, and the separated solution enters the solution boiler 11 through a solution outlet 25 at the bottom of the boiling liquid separator 12 for continuous circulation;
s7, an electric regulating valve 22 is installed on a pipeline branch pipeline of the barren liquor pump 9, the electric regulating valve 22 is interlocked with a liquid level detection system 21 installed on the boiling liquid separator 12, and when the liquid level of the boiling liquid separator 12 is too high, the opening degree of the electric regulating valve 22 is reduced; when the liquid level of the boiling liquid separator 12 is too low, the opening degree of the electric regulating valve 22 is increased, so that stable circulation of the boiling separation system 12 is realized, and the absorbent lean and rich liquid is recycled.
EXAMPLE III
As shown in fig. 1, a flue gas CO is provided for one embodiment of the present invention2The hypergravity regeneration energy-saving process of the trapping system comprises the following steps:
S1.CO2absorption of (2): carrying out desulfurization, denitrification and dust removal on flue gas discharged by a coal-fired power plant through a deep purification tower 1; controlling the temperature of the discharged flue gas to be 37 ℃; the flue gas is pressurized by the draught fan 4Then enters the absorption tower 3 from bottom to top, the barren liquor absorbent enters the absorption tower from top to bottom, and the barren liquor absorbent and the absorption tower are in countercurrent contact to finish CO2The absorption process of (2);
s2, heat exchange: the decarbonized flue gas is discharged from a tail gas discharge port 5 at the top of the absorption tower, and CO is absorbed2The rich solution of the gas is discharged from the bottom of the absorption tower, and the cold rich solution pressurized by the rich solution pump 6 enters the lean rich solution heat exchanger 8 for heat exchange at the temperature of 53 ℃. The temperature of the cold rich liquid after heat exchange is 93 ℃;
S3.CO2desorption: spraying the cold rich liquid after heat exchange into a supergravity reactor 10, and strengthening the relative speed and mutual contact between phases by utilizing the flowing behavior of a multi-phase flow system under the supergravity condition, thereby realizing the mass and heat transfer process and the chemical reaction process, and leading CO to be subjected to the reaction2Rapid desorption from the absorbent;
s4, cooling: the desorbed regeneration gas enters a regeneration gas separator 13 through a regeneration gas outlet 17 and is separated to obtain product gas; the desorbed barren solution is pressurized by a barren solution outlet 18 of the supergravity reactor through a barren solution pump 9 and then enters a barren and rich solution heat exchanger 8 for heat exchange and cooling, wherein the temperature of the heat exchange and cooling of the barren solution is 58 ℃; after cooling, the lean solution enters a lean solution cooler 7 for cooling, and the temperature of the lean solution after being cooled by the lean solution cooler 7 is 43 ℃. The cooled barren solution enters an absorption tower 3 and starts a new absorption process;
s5, synchronous operation: part of the lean solution flows into the siphon-type solution boiler 11 via the electric control valve 22 on the branch of the pipeline of the high-gravity reactor lean solution pump for heating, and the solution boiler 11 can be heated by electric heating or steam heating. Heated solution and CO desorbed during heating2Mixing gas phase and liquid phase, and introducing the mixture into a boiling liquid separator 12 from a boiling liquid outlet 19 for gas-liquid separation under the siphoning action of a solution boiler 11;
s6, post-processing: the separated desorption gas enters the super-gravity reactor 10 from a gas outlet 24 at the top of the boiling liquid separator 12, and the separated solution enters the solution boiler 11 through a solution outlet 25 at the bottom of the boiling liquid separator 12 for continuous circulation;
s7, an electric regulating valve 22 is installed on a pipeline branch pipeline of the barren liquor pump 9, the electric regulating valve 22 is interlocked with a liquid level detection system 21 installed on the boiling liquid separator 12, and when the liquid level of the boiling liquid separator 12 is too high, the opening degree of the electric regulating valve 22 is reduced; when the liquid level of the boiling liquid separator 12 is too low, the opening degree of the electric regulating valve 22 is increased, so that stable circulation of the boiling separation system 12 is realized, and the absorbent lean and rich liquid is recycled.
Example four
As shown in fig. 1, a flue gas CO is provided for one embodiment of the present invention2The hypergravity regeneration energy-saving process of the trapping system comprises the following steps:
S1.CO2absorption of (2): carrying out desulfurization, denitrification and dust removal on flue gas discharged by a coal-fired power plant through a deep purification tower 1; controlling the temperature of the discharged flue gas to be 39 ℃; the flue gas enters the absorption tower 3 from bottom to top after being pressurized by the induced draft fan 4, the barren liquor absorbent enters the absorption tower from top to bottom, and the barren liquor absorbent and the absorption tower are in countercurrent contact to finish CO2The absorption process of (2);
s2, heat exchange: the decarbonized flue gas is discharged from a tail gas discharge port 5 at the top of the absorption tower, and CO is absorbed2The rich solution of the gas is discharged from the bottom of the absorption tower, and the cold rich solution pressurized by the rich solution pump 6 enters the lean rich solution heat exchanger 8 for heat exchange at the temperature of 54 ℃. The temperature of the cold rich liquid after heat exchange is 94 ℃;
S3.CO2desorption: spraying the cold rich liquid after heat exchange into a supergravity reactor 10, and strengthening the relative speed and mutual contact between phases by utilizing the flowing behavior of a multi-phase flow system under the supergravity condition, thereby realizing the mass and heat transfer process and the chemical reaction process, and leading CO to be subjected to the reaction2Rapid desorption from the absorbent;
s4, cooling: the desorbed regeneration gas enters a regeneration gas separator 13 through a regeneration gas outlet 17 and is separated to obtain product gas; the desorbed barren solution is pressurized by a barren solution outlet 18 of the supergravity reactor through a barren solution pump 9 and then enters a barren and rich solution heat exchanger 8 for heat exchange and cooling, wherein the temperature of the heat exchange and cooling of the barren solution is 59 ℃; and cooling the lean solution in a lean solution cooler 7, wherein the temperature of the lean solution cooled by the lean solution cooler 7 is 44 ℃. The cooled barren solution enters an absorption tower 3 and starts a new absorption process;
s5, synchronous operation: part of the barren solution is reacted by supergravityElectric control valve 22 on the pipe branch of the lean solution removal pump flows into siphon-type solution boiler 11 for heating, and the heating form of solution boiler 11 can be electric heating or steam heating. Heated solution and CO desorbed during heating2Mixing gas phase and liquid phase, and introducing the mixture into a boiling liquid separator 12 from a boiling liquid outlet 19 for gas-liquid separation under the siphoning action of a solution boiler 11;
s6, post-processing: the separated desorption gas enters the super-gravity reactor 10 from a gas outlet 24 at the top of the boiling liquid separator 12, and the separated solution enters the solution boiler 11 through a solution outlet 25 at the bottom of the boiling liquid separator 12 for continuous circulation;
s7, an electric regulating valve 22 is installed on a pipeline branch pipeline of the barren liquor pump 9, the electric regulating valve 22 is interlocked with a liquid level detection system 21 installed on the boiling liquid separator 12, and when the liquid level of the boiling liquid separator 12 is too high, the opening degree of the electric regulating valve 22 is reduced; when the liquid level of the boiling liquid separator 12 is too low, the opening degree of the electric regulating valve 22 is increased, so that stable circulation of the boiling separation system 12 is realized, and the absorbent lean and rich liquid is recycled.
EXAMPLE five
As shown in fig. 1, a flue gas CO is provided for one embodiment of the present invention2The hypergravity regeneration energy-saving process of the trapping system comprises the following steps:
S1.CO2absorption of (2): carrying out desulfurization, denitrification and dust removal on flue gas discharged by a coal-fired power plant through a deep purification tower 1; controlling the temperature of the discharged flue gas to be 45 ℃; the flue gas enters the absorption tower 3 from bottom to top after being pressurized by the induced draft fan 4, the barren liquor absorbent enters the absorption tower from top to bottom, and the barren liquor absorbent and the absorption tower are in countercurrent contact to finish CO2The absorption process of (2);
s2, heat exchange: the decarbonized flue gas is discharged from a tail gas discharge port 5 at the top of the absorption tower, and CO is absorbed2The rich solution of the gas is discharged from the bottom of the absorption tower, and the cold rich solution pressurized by the rich solution pump 6 enters the lean rich solution heat exchanger 8 for heat exchange at the temperature of 55 ℃. The temperature of the cold rich liquid after heat exchange is 95 ℃;
S3.CO2desorption: spraying the cold rich liquid after heat exchange into a hypergravity reactor 10, and utilizing a multiphase flow system under the hypergravity conditionThe relative speed and mutual contact between the reinforced phases and the mutual contact are enhanced, thereby realizing the mass and heat transfer process and the chemical reaction process, and leading CO to be in contact with the heat exchange medium2Rapid desorption from the absorbent;
s4, cooling: the desorbed regeneration gas enters a regeneration gas separator 13 through a regeneration gas outlet 17 and is separated to obtain product gas; the desorbed barren solution is pressurized by a barren solution outlet 18 of the supergravity reactor through a barren solution pump 9 and then enters a barren and rich solution heat exchanger 8 for heat exchange and cooling, wherein the temperature of the heat exchange and cooling of the barren solution is 65 ℃; and cooling the lean solution in a lean solution cooler 7, wherein the temperature of the lean solution cooled by the lean solution cooler 7 is 45 ℃. The cooled barren solution enters an absorption tower 3 and starts a new absorption process;
s5, synchronous operation: part of the lean solution flows into the siphon-type solution boiler 11 via the electric control valve 22 on the branch of the pipeline of the high-gravity reactor lean solution pump for heating, and the solution boiler 11 can be heated by electric heating or steam heating. Heated solution and CO desorbed during heating2Mixing gas phase and liquid phase, and introducing the mixture into a boiling liquid separator 12 from a boiling liquid outlet 19 for gas-liquid separation under the siphoning action of a solution boiler 11;
s6, post-processing: the separated desorption gas enters the super-gravity reactor 10 from a gas outlet 24 at the top of the boiling liquid separator 12, and the separated solution enters the solution boiler 11 through a solution outlet 25 at the bottom of the boiling liquid separator 12 for continuous circulation;
s7, an electric regulating valve 22 is installed on a pipeline branch pipeline of the barren liquor pump 9, the electric regulating valve 22 is interlocked with a liquid level detection system 21 installed on the boiling liquid separator 12, and when the liquid level of the boiling liquid separator 12 is too high, the opening degree of the electric regulating valve 22 is reduced; when the liquid level of the boiling liquid separator 12 is too low, the opening degree of the electric regulating valve 22 is increased, so that stable circulation of the boiling separation system 12 is realized, and the absorbent lean and rich liquid is recycled.
The invention provides a supergravity regeneration energy-saving process for a flue gas CO2 trapping system in the above embodiment, the invention improves the existing organic amine chemical absorption process, adopts a supergravity machine to replace a conventional desorption tower to heat and regenerate absorption liquid, and can realize the miniaturization of a desorption systemFlexible, skid-mounted and modular. Firstly proposes the chemical absorption method for flue gas CO2The trapping system adopts a coupled regeneration process of the hypergravity reactor, the solution boiler and the boiling liquid separator to replace the original regeneration process of the desorption tower and the boiling device, so that the size of equipment is greatly reduced, and the device has the advantages of miniaturization, flexibility, high efficiency, small investment, skid-mounted equipment, modularization and the like, saves the investment cost and obviously reduces the regeneration energy consumption. Chemical absorption method for flue gas CO2The coupled regeneration process of the 'super-gravity reactor, the solution boiler and the boiling liquid separator' of the trapping system reduces the medicament loss and the degradation and deterioration of the medicament, improves the recycling times of the chemical absorbent, meets the characteristics of low consumption, low emission and high efficiency of recycling economy, and achieves the purposes of recycling and reducing environmental pollution.
The above description is only for the purpose of illustrating the preferred embodiments of the present invention and is not to be construed as limiting the invention, and any modifications, equivalents and improvements made within the spirit and principle of the present invention are intended to be included within the scope of the present invention.
Claims (7)
1. Flue gas CO2The hypergravity regeneration energy-saving process of the trapping system is characterized by comprising the following steps:
S1.CO2absorption of (2): carrying out desulfurization, denitrification and dust removal on flue gas discharged by a coal-fired power plant through a deep purification tower; controlling the temperature of the discharged flue gas; the flue gas enters the absorption tower from bottom to top after being pressurized by the induced draft fan, the barren liquor absorbent enters the absorption tower from top to bottom, and the barren liquor absorbent and the absorption tower are in countercurrent contact to finish CO2The absorption process of (2);
s2, heat exchange: the decarbonized flue gas is discharged from a tail gas discharge port at the top of the absorption tower, and CO is absorbed2Discharging a rich solution of the gas from the bottom of the absorption tower, and introducing a cold rich solution pressurized by a rich solution pump into a lean rich solution heat exchanger for heat exchange, wherein the temperature of the cold rich solution after heat exchange is 90-95 ℃;
S3.CO2desorption: spraying the cold rich liquid after heat exchange into a supergravity reactor, and strengthening the relative phase-to-phase ratio by utilizing the flowing behavior of a multiphase flow system under the supergravity conditionSpeed and mutual contact, thereby realizing mass and heat transfer processes and chemical reaction processes to make CO2Rapid desorption from the absorbent;
s4, cooling: the desorbed regeneration gas enters a regeneration gas separator through a regeneration gas outlet to be separated to obtain product gas; the desorbed barren solution is pressurized by a barren solution pump from a barren solution outlet of the supergravity reactor and then enters a barren and rich solution heat exchanger for heat exchange and cooling; cooling the lean solution in a lean solution cooler, feeding the cooled lean solution into an absorption tower, and starting a new absorption process;
s5, synchronous operation: part of the barren solution flows into the siphon type solution boiler through an electric regulating valve on a pipeline branch of the barren solution pump of the supergravity reactor to be heated, and the heated solution and CO desorbed in the heating process2Mixing gas phase and liquid phase, and introducing the mixture into a boiling liquid separator from a boiling liquid outlet under the siphoning action of a solution boiler for gas-liquid separation;
s6, post-processing: the separated desorption gas enters the super-gravity reactor from a gas outlet at the top of the boiling liquid separator, and the separated solution enters the solution boiler through a solution outlet at the bottom of the boiling liquid separator to be continuously circulated;
s7, an electric regulating valve is installed on a pipeline branch line of the barren liquid pump pipeline and interlocked with a liquid level detection system installed on the boiling liquid separator, and when the liquid level of the boiling liquid separator is too high, the opening degree of the electric regulating valve is reduced; when the liquid level of the boiling liquid separator is too low, the opening of the electric regulating valve is increased, so that the stable circulation of the boiling separation system is realized.
2. The flue gas CO of claim 12The hypergravity regeneration energy-saving process of the trapping system is characterized in that the temperature of the flue gas is 35-45 ℃ according to S1.
3. The flue gas CO of claim 12The hypergravity regeneration energy-saving process of the trapping system is characterized in that the temperature of the cold rich liquid is 50-55 ℃ according to S1.
4. According to the rightFlue gas CO according to claim 12The hypergravity regeneration energy-saving process of the trapping system is characterized in that according to S4, the heat exchange cooling temperature of the barren solution is 55-65 ℃.
5. The flue gas CO of claim 42The hypergravity regeneration energy-saving process of the trapping system is characterized in that the temperature of the barren solution after the barren solution is cooled by a barren solution cooler 7 is 40-45 ℃.
6. The flue gas CO of claim 12The capture system hypergravity regeneration energy saving process, characterized in that the heating form of the solution boiler may be electric heating or steam heating according to S5.
7. The flue gas CO of claim 12The capture system hypergravity regeneration energy saving process is characterized in that according to S7, the absorbent lean-rich solution is recycled.
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