CN115523004B - Amine process CO 2 Combined power generation device and method for recovering heat energy of process medium in trapping device - Google Patents
Amine process CO 2 Combined power generation device and method for recovering heat energy of process medium in trapping device Download PDFInfo
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- 238000000034 method Methods 0.000 title claims abstract description 78
- 150000001412 amines Chemical class 0.000 title claims abstract description 68
- 238000010248 power generation Methods 0.000 title claims abstract description 37
- 239000003507 refrigerant Substances 0.000 claims abstract description 272
- 239000002918 waste heat Substances 0.000 claims abstract description 123
- 238000011084 recovery Methods 0.000 claims abstract description 117
- 238000011069 regeneration method Methods 0.000 claims abstract description 67
- 230000008929 regeneration Effects 0.000 claims abstract description 66
- 239000007788 liquid Substances 0.000 claims abstract description 61
- 238000010521 absorption reaction Methods 0.000 claims abstract description 58
- 238000005057 refrigeration Methods 0.000 claims abstract description 53
- 239000007789 gas Substances 0.000 claims abstract description 49
- 238000010992 reflux Methods 0.000 claims abstract description 48
- 230000005611 electricity Effects 0.000 claims abstract description 21
- 238000001704 evaporation Methods 0.000 claims abstract description 12
- 239000012071 phase Substances 0.000 claims description 45
- 239000006096 absorbing agent Substances 0.000 claims description 11
- 238000010438 heat treatment Methods 0.000 claims description 11
- 239000007791 liquid phase Substances 0.000 claims description 11
- 238000009833 condensation Methods 0.000 claims description 10
- 238000001816 cooling Methods 0.000 claims description 9
- 230000001172 regenerating effect Effects 0.000 claims description 6
- 238000004891 communication Methods 0.000 claims description 3
- 238000009835 boiling Methods 0.000 claims 2
- 239000000498 cooling water Substances 0.000 abstract description 4
- 230000008020 evaporation Effects 0.000 abstract description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 239000003209 petroleum derivative Substances 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
- F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
- F01K27/00—Plants for converting heat or fluid energy into mechanical energy, not otherwise provided for
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
- F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
- F01K11/00—Plants characterised by the engines being structurally combined with boilers or condensers
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
- F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
- F01K25/00—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for
- F01K25/08—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for using special vapours
- F01K25/10—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for using special vapours the vapours being cold, e.g. ammonia, carbon dioxide, ether
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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
- F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
- F25B9/00—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point
- F25B9/002—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point characterised by the refrigerant
- F25B9/008—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point characterised by the refrigerant the refrigerant being 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
- 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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Abstract
The invention provides an amine method CO 2 The combined power generation device for recovering heat energy of process medium in the trapping device comprises a refrigerant reflux valve group, a refrigerant expansion generator I, a refrigerant condenser I, a refrigerant storage tank I, a refrigerant booster pump I, a refrigerant distribution valve group, an amine liquid regeneration tower waste heat recovery heat exchanger and CO 2 Compressor unit outlet waste heat recovery heat exchanger and CO 2 The outlet waste heat recovery heat exchanger of the refrigeration compressor. The device adopts the refrigerant to replace cooling water, and utilizes the phase change evaporation latent heat of the refrigerant to carry out CO 2 Gas outlet from top of absorption tower, gas outlet from top of amine liquid regeneration tower and CO 2 Refrigerant compressor outlet refrigerant and CO 2 The process medium at the outlet of the compressor is cooled, the gas phase evaporated by the refrigerant is utilized for expansion power generation, the process of generating power by utilizing the recovered heat energy while the process medium is cooled is realized, and CO can be recovered 2 The heat energy of 8-15% of the trapping device is used for generating electricity, and CO is reduced 2 And (5) collecting cost. The invention also provides a method for using the device.
Description
Technical Field
The present invention relates to CO 2 The technical field of trapping, in particular to an amine method CO 2 A process medium heat energy recovery combined power generation device and a process medium heat energy recovery combined power generation method in a trapping device.
Background
CO capture in the amine process is currently being performed 2 In the process, the heat energy of the gas at the top of the amine liquid regeneration tower, the heat energy of the liquid at the bottom of the regeneration tower and the heat energy at the outlet of the compressor are all required to be cooled by cooling water, and the heat energy can only be wasted through the cooling water tower, so that a large amount of energy is wasted. Along with CO 2 The continuous construction of the trapping device causes more and more energy waste, and the recovery of the waste heat of the processes of the types can reduce CO 2 An efficient means of capturing costs.
Disclosure of Invention
To solve the technical problems, the invention aims toProviding an amine process CO 2 And the device is used for collecting heat energy of the process medium in the device and combining the heat energy recovery of the process medium with the power generation device so as to realize the cooling of the process medium and simultaneously utilize the recovered heat energy to generate power. The invention also provides a CO method using the amine method 2 A method for recovering heat energy of process medium in a trapping device and a combined power generation device.
The technical scheme adopted by the invention is as follows:
amine method CO 2 The combined power generation device for recovering heat energy of process medium in the trapping device comprises a refrigerant reflux valve group, a refrigerant expansion generator I, a refrigerant condenser I, a refrigerant storage tank I, a refrigerant booster pump I, a refrigerant distribution valve group, an amine liquid regeneration tower waste heat recovery heat exchanger and CO 2 Compressor unit outlet waste heat recovery heat exchanger and CO 2 An outlet waste heat recovery heat exchanger of the refrigeration compressor; the outlet of the refrigerant reflux valve bank is sequentially communicated with a refrigerant expansion generator I, a refrigerant condenser I, a refrigerant storage tank I, a refrigerant booster pump I and a refrigerant distribution valve bank through pipelines, the refrigerant distribution valve bank comprises three distribution valves, and the three distribution valves are respectively communicated with an amine liquid regeneration tower waste heat recovery heat exchanger and CO through pipelines 2 Compressor unit outlet waste heat recovery heat exchanger and CO 2 The cold end of the refrigeration compressor outlet waste heat recovery heat exchanger is communicated; regeneration tower waste heat recovery heat exchanger and CO 2 Compressor unit outlet waste heat recovery heat exchanger and CO 2 And the hot end outlet of the refrigeration compressor outlet waste heat recovery heat exchanger is respectively communicated with three reflux valves of the refrigerant reflux valve group through pipelines.
The amine method CO 2 The process medium heat recovery combined power generation device in the trapping device further comprises a second refrigerant expansion generator, a second refrigerant condenser, a second refrigerant storage tank, a second refrigerant booster pump and an absorber waste heat recovery heat exchanger; and the outlet of the second refrigerant expansion generator is sequentially communicated with the second refrigerant condenser, the second refrigerant storage tank, the second refrigerant booster pump, the absorber waste heat recovery heat exchanger and the inlet of the second refrigerant expansion generator through pipelines.
The amine method CO 2 Trapping device middling workCombined power generation device for heat energy recovery of process medium, wherein CO 2 The outlet of the refrigeration compressor is connected with CO in turn through a pipeline 2 Hot end, valve and CO of refrigerating compressor outlet waste heat recovery heat exchanger 2 Cold end inlet and CO of refrigeration heat exchanger 2 The population of the refrigeration compressor is communicated.
The amine method CO 2 The process medium heat recovery combined power generation device in the trapping device, wherein the top of the amine liquid regeneration tower is sequentially communicated with the hot end inlet of the regeneration tower waste heat recovery heat exchanger through a pipeline, the cold end outlet of the regeneration tower waste heat recovery heat exchanger is sequentially communicated with the upper part of the regeneration tower top reflux tank through a pipeline, and the bottom of the regeneration tower top reflux tank is sequentially communicated with the regeneration tower top reflux pump and the upper part of the amine liquid regeneration tower through pipelines.
The amine method CO 2 The process medium heat energy recovery combined power generation device in the trapping device, wherein the top of a reflux tank at the top of the regeneration tower is sequentially connected with CO through a pipeline 2 Compressor, CO 2 Hot end and CO of compressor unit outlet waste heat recovery heat exchanger 2 Hot side inlet and CO for refrigeration heat exchanger 2 The output pipeline is communicated.
The amine method CO 2 Combined power generation device for recovering heat energy of process medium in trapping device, wherein CO 2 The top of the absorption tower is sequentially connected with the waste heat recovery heat exchanger of the absorption tower, the upper part of the reflux tank at the top of the absorption tower and CO through pipelines 2 The upper part of the side wall of the absorption tower is communicated.
The amine method CO 2 Combined power generation device for recovering heat energy of process medium in trapping device, wherein reflux tank and CO at top of absorption tower 2 And a pipeline between the absorption towers is provided with an absorption tower top reflux pump.
CO using the amine method of the invention 2 The method for recovering the heat energy of the process medium in the trapping device and combining the power generation device comprises the following steps of:
amine liquid regenerating tower and compressor waste heat recovery
The refrigerants stored in the first refrigerant storage tank are pressurized by the first refrigerant booster pump and then respectively enter:
1)CO 2 the cold end of the regeneration tower top waste heat recovery heat exchanger and the amine liquid regeneration tower at the hot end eject CO 2 The gas exchanges heat to exchange CO at the top of the tower 2 Cooling the gas, evaporating the liquid refrigerant by utilizing the residual heat of the tower top, and heating the gas-phase refrigerant;
2)CO 2 cold end of waste heat recovery heat exchanger at outlet of refrigeration booster compressor, and CO 2 High temperature R507 at the outlet of the refrigeration compressor exchanges heat to exchange CO 2 The outlet gas of the refrigeration compressor is cooled and at the same time, CO is utilized 2 Evaporating liquid refrigerant by using waste heat at the outlet of the refrigeration compressor, and heating the gas-phase refrigerant;
3)CO 2 the cold end of the heat exchanger for recovering waste heat at the outlet of the booster compressor is connected with CO 2 High temperature CO at compressor outlet 2 Heat exchange is carried out to CO 2 Compressor outlet gas cooling, while utilizing CO 2 Evaporating the liquid refrigerant by using waste heat of the outlet of the compressor, and heating the gas-phase refrigerant;
the gas phases of the refrigerants evaporated and vaporized by the three heat exchangers are collected and enter a first refrigerant expansion generator to generate power, the gas phase refrigerants after expansion and power generation are cooled into liquid phases by a first refrigerant condenser and flow back to a first refrigerant storage tank, so that a heat exchange-gasification-expansion power generation-condensation cycle of the refrigerants is completed;
(II) CO 2 Waste heat recovery of absorption tower
The refrigerant stored in the second refrigerant storage tank is pressurized by the second refrigerant booster pump and then enters the waste heat recovery heat exchanger of the absorption tower to be in contact with CO at the hot end 2 The gas ejected from the absorption tower exchanges heat to cool the gas at the top of the tower, and at the same time, CO is utilized 2 The waste heat at the top of the absorption tower evaporates the liquid refrigerant, heats the gas-phase refrigerant, enters a refrigerant expansion generator II to generate power, and the gas-phase refrigerant after expansion power generation is cooled into a liquid phase through a refrigerant condenser II and flows back to a refrigerant storage tank II, so that the heat exchange-gasification-expansion power generation-condensation cycle of the refrigerant is completed.
The amine method CO 2 A method of capturing process media heat energy in a process media heat recovery cogeneration unit comprising the steps of:
amine liquid regenerating tower and compressor waste heat recovery
The refrigerant of 35 ℃ stored in the first refrigerant storage tank is pressurized to 800kPa by the first refrigerant booster pump and then enters into the first refrigerant storage tank respectively:
1)CO 2 the cold end of the regeneration tower top waste heat recovery heat exchanger and the amine liquid regeneration tower at the hot end eject CO 2 The gas exchanges heat to exchange CO at the top of the tower 2 Cooling the gas to 40 ℃, at the same time, evaporating the liquid refrigerant by utilizing the residual heat of the tower top, and heating the gas-phase refrigerant to 100-102 ℃;
2)CO 2 cold end of waste heat recovery heat exchanger at outlet of refrigeration booster compressor, and CO 2 High temperature R507 at the outlet of the refrigeration compressor exchanges heat to exchange CO 2 The refrigerant compressor outlet gas is cooled to 40 ℃ while utilizing CO 2 Evaporating liquid refrigerant by using waste heat at the outlet of the refrigeration compressor, and heating the temperature of the gas-phase refrigerant to 105 ℃;
3)CO 2 the cold end of the heat exchanger for recovering waste heat at the outlet of the booster compressor is connected with CO 2 High temperature CO at compressor outlet 2 Heat exchange is carried out to CO 2 The compressor outlet gas is cooled to 40 ℃ while at the same time utilizing CO 2 Evaporating the liquid refrigerant by using waste heat of the outlet of the compressor, and heating the temperature of the gas-phase refrigerant to 115 ℃;
the gas phases of the refrigerants evaporated and vaporized by the three heat exchangers are collected, the temperature is about 103-108 ℃, the pressure is 780-3350kPa, the refrigerant enters a first refrigerant expansion generator to generate electricity, the electricity generation power is 1850-2039kW, the temperature of the gas phase refrigerant after expansion and electricity generation is about 50.7-57 ℃, the pressure is 180-1000kPa, the gas phase refrigerant is cooled to a liquid phase by a first refrigerant condenser, the temperature is 35 ℃, and the gas phase refrigerant flows back to a first refrigerant storage tank, so that the heat exchange-gasification-expansion electricity generation-condensation cycle of the refrigerant is completed;
(II) CO 2 Waste heat recovery of absorption tower
Stored in refrigerant tank two at 35 cThe refrigerant enters the waste heat recovery heat exchanger of the absorption tower after being boosted by the refrigerant booster pump by 350-3400kPa, and is reacted with CO at the hot end 2 The gas ejected from the absorption tower exchanges heat, the gas at the top of the absorption tower is cooled to 40 ℃, and at the same time, CO is utilized 2 The waste heat at the top of the absorption tower evaporates the liquid refrigerant, heats the gas-phase refrigerant to 65 ℃, enters the second refrigerant expansion generator to generate electricity with the electricity generation power of 700-755kW, expands the gas-phase refrigerant after electricity generation to have the temperature of about 43.5-48.4 ℃ and the pressure of 160-1000kPa, then cools the gas-phase refrigerant into a liquid phase through the second refrigerant condenser to have the temperature of 35 ℃ and returns to the second refrigerant storage tank, thereby completing the heat exchange-gasification-expansion electricity generation-condensation cycle of one refrigerant.
The amine method CO 2 The method for the combined power generation device for recovering the heat energy of the process medium in the trapping device comprises the steps of (1) and (two), wherein the refrigerant adopted in the step (two) is a low-boiling-point refrigerant, and the low-boiling-point refrigerant is one of R11 and R134 a.
The invention has the beneficial effects that:
the amine method CO 2 The process medium heat recovery combined power generation device in the trapping device adopts a refrigerant to replace cooling water, and utilizes the phase change evaporation latent heat of the refrigerant to carry out CO 2 Gas outlet from top of absorption tower, gas outlet from top of amine liquid regeneration tower and CO 2 Refrigerant compressor outlet refrigerant and CO 2 The process medium at the outlet of the compressor is cooled, the gas phase evaporated by the refrigerant is utilized for expansion power generation, the process of generating power by utilizing the recovered heat energy while the process medium is cooled is realized, and CO can be recovered 2 The heat energy of 8-15% of the trapping device is used for generating electricity, and CO is reduced 2 And (5) collecting cost.
The amine method CO 2 Combined power generation device for recovering heat energy of process medium in trapping device, and can be used for CO 2 Besides the heat energy recovery in the technical process of the amine method trapping device, the device is also suitable for cooling, recovering and generating high-temperature materials at the parts of a regenerating tower, a compressor and the like of a petrochemical device, a petroleum and natural gas treatment device and the like.
Drawings
FIG. 1 is an amine according to the inventionProcess CO 2 And a structural schematic diagram of the process medium heat energy recovery combined power generation device in the trapping device.
In the figure, a 1-refrigerant return valve group; 2-refrigerant expansion generator one; 3-refrigerant condenser one; 4-refrigerant tank one; 5-a first refrigerant booster pump; 6-refrigerant distribution valve group; 7-amine liquid regeneration tower waste heat recovery heat exchanger; 8-CO 2 The waste heat recovery heat exchanger at the outlet of the compressor unit; 9-CO 2 An outlet waste heat recovery heat exchanger of the refrigeration compressor; 10-a second refrigerant expansion generator; 11-refrigerant condenser two; 12-a second refrigerant storage tank; 13-a refrigerant booster pump II; 14-an absorber waste heat recovery heat exchanger; 15-CO 2 An absorption tower; 16-an absorber overhead reflux drum; 17-an absorber overhead reflux pump; an 18-amine liquid regeneration tower; 19-valve; 20-CO 2 A refrigeration compressor; 21-CO 2 A refrigeration heat exchanger; 22-CO 2 A compressor; 23-a regeneration overhead reflux drum; 24-regeneration tower top reflux pump
The invention will be further described with reference to specific examples and figures.
Detailed Description
Example 1
As shown in FIG. 1, an amine process CO 2 The combined power generation device for recovering heat energy of process medium in the trapping device comprises a refrigerant reflux valve group 1, a refrigerant expansion generator 1, a refrigerant condenser 3, a refrigerant storage tank 4, a refrigerant booster pump 5, a refrigerant distribution valve group 6, an amine liquid regeneration tower heat recovery heat exchanger 7 and CO 2 Compressor unit outlet waste heat recovery heat exchanger 8, CO 2 The system comprises a refrigeration compressor outlet waste heat recovery heat exchanger 9, a second refrigerant expansion generator 10, a second refrigerant condenser 11, a second refrigerant storage tank 12, a second refrigerant booster pump 13 and an absorption tower waste heat recovery heat exchanger 14.
The outlet of the refrigerant reflux valve group 1 is sequentially communicated with a refrigerant expansion generator I2, a refrigerant condenser I3, a refrigerant storage tank I4, a refrigerant booster pump I5 and a refrigerant distribution valve group 6 through pipelines, the refrigerant distribution valve group 6 comprises three distribution valves, and the three distribution valves are respectively communicated with an amine liquid regeneration tower waste heat recovery heat exchanger 7 and CO through pipelines 2 Compressor unit outlet waste heat recoveryHeat exchanger 8 and CO 2 The cold end of the refrigeration compressor outlet waste heat recovery heat exchanger 9 is communicated; regeneration tower waste heat recovery heat exchanger 7 and CO 2 Compressor unit outlet waste heat recovery heat exchanger 8 and CO 2 And the hot end outlet of the refrigeration compressor outlet waste heat recovery heat exchanger 9 is respectively communicated with three reflux valves of the refrigerant reflux valve group 1 through pipelines.
And also includes CO 2 The refrigerating unit comprises a valve 19 and CO 2 Refrigeration compressor 20 and CO 2 Refrigeration heat exchanger 21, CO 2 The outlet of the refrigeration compressor 20 is connected with CO in turn by a pipeline 2 Hot end of refrigeration compressor outlet waste heat recovery heat exchanger 9, valve 19, CO 2 Cold side inlet and CO of refrigeration heat exchanger 21 2 The refrigerant compressor 20 is in communication with the population.
The top of the amine liquid regeneration tower 18 is sequentially communicated with the hot end inlet of the regeneration tower waste heat recovery heat exchanger 7 through a pipeline, the cold end outlet of the regeneration tower waste heat recovery heat exchanger 7 is sequentially communicated with the upper part of the regeneration tower top reflux tank 23 through a pipeline, and the bottom of the regeneration tower top reflux tank 23 is sequentially communicated with the regeneration tower top reflux pump 24 and the upper part of the amine liquid regeneration tower 18 through a pipeline.
The top of the regeneration tower top reflux drum 23 is connected with CO in turn through a pipeline 2 Compressor 22, CO 2 Hot end and CO of compressor unit outlet waste heat recovery heat exchanger 8 2 Hot side inlet and CO of refrigeration heat exchanger 21 2 The output pipeline is communicated.
The outlet of the second refrigerant expansion generator 10 is sequentially communicated with the second refrigerant condenser 11, the second refrigerant storage tank 12, the second refrigerant booster pump 13, the absorber waste heat recovery heat exchanger 14 and the inlet of the second refrigerant expansion generator 10 through pipelines.
CO 2 The top of the absorption tower 15 is sequentially connected with the waste heat recovery heat exchanger 14 of the absorption tower, the upper part of the reflux tank 16 of the top of the absorption tower and CO through pipelines 2 The upper part of the side wall of the absorption tower 15 is communicated with the reflux tank 16 at the top of the absorption tower and CO 2 An absorption tower top reflux pump 17 is arranged on a pipeline between the absorption towers 15.
The amine method CO described in this example 2 Specific engineering of process medium heat energy recovery combined power generation device in trapping deviceThe preparation process comprises the following steps:
in the embodiment, R11 is taken as a waste heat absorbing refrigerant to recycle CO 2 Absorption tower 15, amine liquid regeneration tower 18, and CO 2 Compressor 22 and CO 2 The waste heat of the refrigerant compressor 20.
Amine liquid regenerating tower and compressor waste heat recovery
The amine liquid regeneration tower 18 is vented:
(1) The components are as follows: CO 2 -50％、Nitrogen-0.1％、H 2 O-49.9％；
(2) Temperature: 102 ℃;
(3) Flow rate: 53.1t/h
(4) Total power of waste heat: 10.89MW (cooled to 40 ℃ C.)
CO 2 Compressor 22:
(1) Flow rate: 38.34t/h;
(2) Temperature: 117-122 ℃;
(3) Total power of waste heat: 2.2MW (cooling to 40 ℃ C. Basis);
CO 2 refrigeration compressor 20:
(1) Refrigerant: r507
(2) Flow rate: 128t/h;
(3) Temperature: 106 ℃;
(4) Total power of waste heat: 6.74MW (cooled to 40 ℃ C. As a benchmark)
The R11 refrigerant of 35 ℃ stored in the first refrigerant storage tank 4 is pressurized to 800kPa by the first refrigerant booster pump 5 and then enters into the first refrigerant storage tank:
1)CO 2 the cold end of the regeneration tower top waste heat recovery heat exchanger 7 and the amine liquid regeneration tower 18 at the hot end are used for ejecting CO 2 The gas exchanges heat to exchange CO at the top of the tower 2 The gas is cooled to 40 c while the liquid cryogen is vaporized by the overhead heat and the gas-phase cryogen is heated to 100 c.
2)CO 2 Cold end of outlet waste heat recovery heat exchanger 9 of refrigerating booster compressor, and CO 2 High temperature R507 at the outlet of the refrigeration compressor 20 exchanges heat to exchange CO 2 The refrigerant compressor 20 outlet gas is cooled to 40 c while at the same time utilizing CO 2 Refrigerating compressorEvaporating the liquid cryogen by using the waste heat of the outlet 20, and heating the gas-phase cryogen to 105 ℃;
3)CO 2 the cold end of the booster compressor outlet waste heat recovery heat exchanger 8 is connected with CO 2 High temperature CO at the compressor 22 outlet 2 Heat exchange is carried out to CO 2 The compressor 22 outlet gas is cooled to 40 c while at the same time utilizing CO 2 The liquid refrigerant is evaporated by the waste heat of the outlet of the compressor 22, and the temperature of the gas-phase refrigerant is heated to 115 ℃;
the gas phases of the refrigerants evaporated and vaporized by the three heat exchangers are collected (the temperature is about 103 ℃ and the pressure is 780 kPa), enter a first refrigerant expansion generator 2 to generate electricity (the power generation power is 2039 kW), the gas phase refrigerant (the temperature is about 57 ℃ and the pressure is 180 kPa) after expansion and power generation is cooled into a liquid phase (the temperature is about 35 ℃) by a first refrigerant condenser 3, and the liquid phase is returned to a first refrigerant storage tank 4, so that the heat exchange-gasification-expansion power generation-condensation cycle of the refrigerant is completed.
(II) CO 2 Waste heat recovery of absorber 15
The waste heat process conditions of the absorption tower are as follows:
(1) The components are as follows: CO 2 -0.67％、Nitrogen-71.6％、Oxygen-4.76％、H 2 O-23％；
(2) Temperature: 66.3 ℃;
(3) Flow rate: 192.4t/h
(4) Total power of waste heat: 16.76MW (cooled to 40 ℃ C. As a benchmark)
R11 refrigerant at 35 ℃ stored in the second refrigerant storage tank 12 enters the absorber waste heat recovery heat exchanger 14 after being pressurized by 350kPa through the second refrigerant booster pump 13, and is reacted with CO at the hot end 2 The gas at the top of the absorption tower 15 exchanges heat, the gas at the top of the absorption tower is cooled to 40 ℃, and at the same time, CO is utilized 2 The residual heat at the top of the absorption tower 15 evaporates the liquid refrigerant, heats the gas-phase refrigerant to 65 ℃, enters the second refrigerant expansion generator 10 to generate electricity (the power generation power is 700 kW), expands the gas-phase refrigerant after the electricity generation (the temperature is about 48.4 ℃ and the pressure is 160 kPa), cools the gas-phase refrigerant into a liquid phase (the temperature is about 35 ℃) through the second refrigerant condenser 11, and returns to the second refrigerant storage tank 12, thereby completing the electricity generationForming a heat exchange-gasification-expansion power generation-condensation cycle of the refrigerant.
Example 2
As shown in FIG. 1, an amine process CO 2 The combined power generation device for recovering heat energy of process medium in the trapping device comprises a refrigerant reflux valve group 1, a refrigerant expansion generator 1, a refrigerant condenser 3, a refrigerant storage tank 4, a refrigerant booster pump 5, a refrigerant distribution valve group 6, an amine liquid regeneration tower heat recovery heat exchanger 7 and CO 2 Compressor unit outlet waste heat recovery heat exchanger 8, CO 2 The system comprises a refrigeration compressor outlet waste heat recovery heat exchanger 9, a second refrigerant expansion generator 10, a second refrigerant condenser 11, a second refrigerant storage tank 12, a second refrigerant booster pump 13 and an absorption tower waste heat recovery heat exchanger 14.
The outlet of the refrigerant reflux valve group 1 is sequentially communicated with a refrigerant expansion generator I2, a refrigerant condenser I3, a refrigerant storage tank I4, a refrigerant booster pump I5 and a refrigerant distribution valve group 6 through pipelines, the refrigerant distribution valve group 6 comprises three distribution valves, and the three distribution valves are respectively communicated with an amine liquid regeneration tower waste heat recovery heat exchanger 7 and CO through pipelines 2 Compressor unit outlet waste heat recovery heat exchanger 8 and CO 2 The cold end of the refrigeration compressor outlet waste heat recovery heat exchanger 9 is communicated; regeneration tower waste heat recovery heat exchanger 7 and CO 2 Compressor unit outlet waste heat recovery heat exchanger 8 and CO 2 And the hot end outlet of the refrigeration compressor outlet waste heat recovery heat exchanger 9 is respectively communicated with three reflux valves of the refrigerant reflux valve group 1 through pipelines.
CO 2 The refrigerating unit comprises a valve 19 and CO 2 Refrigeration compressor 20 and CO 2 Refrigeration heat exchanger 21, CO 2 The outlet of the refrigeration compressor 20 is connected with CO in turn by a pipeline 2 Hot end of refrigeration compressor outlet waste heat recovery heat exchanger 9, valve 19, CO 2 Cold side inlet and CO of refrigeration heat exchanger 21 2 The refrigerant compressor 20 is in communication with the population.
The top of the amine liquid regeneration tower 18 is sequentially communicated with the hot end inlet of the regeneration tower waste heat recovery heat exchanger 7 through a pipeline, the cold end outlet of the regeneration tower waste heat recovery heat exchanger 7 is sequentially communicated with the upper part of the regeneration tower top reflux tank 23 through a pipeline, and the bottom of the regeneration tower top reflux tank 23 is sequentially communicated with the regeneration tower top reflux pump 24 and the upper part of the amine liquid regeneration tower 18 through a pipeline.
The top of the regeneration tower top reflux drum 23 is connected with CO in turn through a pipeline 2 Compressor 22, CO 2 Hot end and CO of compressor unit outlet waste heat recovery heat exchanger 8 2 Hot side inlet and CO of refrigeration heat exchanger 21 2 The output pipeline is communicated.
The outlet of the second refrigerant expansion generator 10 is sequentially communicated with the second refrigerant condenser 11, the second refrigerant storage tank 12, the second refrigerant booster pump 13, the absorber waste heat recovery heat exchanger 14 and the inlet of the second refrigerant expansion generator 10 through pipelines.
CO 2 The top of the absorption tower 15 is sequentially connected with the waste heat recovery heat exchanger 14 of the absorption tower, the upper part of the reflux tank 16 of the top of the absorption tower and CO through pipelines 2 The upper part of the side wall of the absorption tower 15 is communicated with the reflux tank 16 at the top of the absorption tower and CO 2 An absorption tower top reflux pump is arranged on a pipeline between the absorption towers 15.
The amine method CO described in this example 2 The specific working process of the process medium heat energy recovery combined power generation device in the trapping device comprises the following steps:
in the embodiment, R134a is used as a waste heat absorbing refrigerant to recycle CO 2 Absorption tower 15, amine liquid regeneration tower 18, and CO 2 Compressor 22 and CO 2 The waste heat of the refrigerant compressor 20.
Amine liquid regenerating tower and compressor waste heat recovery
The amine liquid regeneration tower 18 is discharged:
(1) The components are as follows: CO 2 -50％、Nitrogen-0.1％、H 2 O-49.9％；
(2) Temperature: 102 ℃;
(3) Flow rate: 53.1t/h
(4) Total power of waste heat: 10.89MW (cooled to 40 ℃ C.)
CO 2 Compressor 22:
(1) Flow rate: 38.34t/h;
(2) Temperature: 117-122 ℃;
(3) Total power of waste heat: 2.2MW (cooling to 40 ℃ C. Basis);
CO 2 refrigeration compressor 20:
(1) Refrigerant: r507
(2) Flow rate: 128t/h;
(3) Temperature: 106 ℃;
(4) Total power of waste heat: 6.74MW (cooled to 40 ℃ C. As a benchmark)
The R134a refrigerant stored in the first refrigerant storage tank 4 at 35 ℃ is increased to 800kPa by the first refrigerant booster pump 5, and then enters into the first refrigerant storage tank:
1)CO 2 the cold end of the regeneration tower top waste heat recovery heat exchanger 7 and the amine liquid regeneration tower 18 at the hot end are used for ejecting CO 2 The gas exchanges heat to exchange CO at the top of the tower 2 Cooling the gas to 40 ℃, at the same time, evaporating the liquid refrigerant by utilizing the residual heat of the tower top, and heating the gas-phase refrigerant to 102 ℃;
2)CO 2 the cold end of the outlet waste heat recovery heat exchanger 9 of the refrigeration booster compressor is connected with CO 2 High temperature R507 at the outlet of the refrigeration compressor 20 exchanges heat to exchange CO 2 The refrigerant compressor 20 outlet gas is cooled to 40 c while at the same time utilizing CO 2 The liquid refrigerant is evaporated by the residual heat at the outlet of the refrigeration compressor 20, and the temperature of the gas-phase refrigerant is heated to 105 ℃;
3)CO 2 the cold end of the booster compressor outlet waste heat recovery heat exchanger 8 is connected with CO 2 High temperature CO at the compressor 22 outlet 2 Heat exchange is carried out to CO 2 The compressor 22 outlet gas is cooled to 40 c while at the same time utilizing CO 2 The liquid refrigerant is evaporated by the waste heat of the outlet of the compressor 22, and the temperature of the gas-phase refrigerant is heated to 115 ℃;
the gas phases of the refrigerants evaporated and vaporized by the three heat exchangers are collected (the temperature is about 108 ℃ and the pressure is 3350 kPa), enter a refrigerant expansion generator I2 to generate electricity (the power 1850 kW), the gas phase refrigerant (the temperature is about 50.7 ℃ and the pressure is 1000 kPa) after expansion and power generation is cooled into a liquid phase (the temperature is about 35 ℃) by a refrigerant condenser I3 and flows back to a refrigerant storage tank I4, so that the heat exchange-gasification-expansion power generation-condensation cycle of the refrigerant is completed.
(II) CO 2 Surplus of absorption tower 15Heat recovery
(1) The components are as follows: CO 2 -0.67％、Nitrogen-71.6％、Oxygen-4.76％、H 2 O-23％；
(2) Temperature: 66.3 ℃;
(3) Flow rate: 192.4t/h
(4) Total power of waste heat: 16.76MW (cooled to 40 ℃ C. As a benchmark)
R134 refrigerant at 35 ℃ stored in the second refrigerant storage tank 12 is pressurized to 3400kPa through the second refrigerant booster pump 13 and then enters the waste heat recovery heat exchanger 14 of the absorption tower to be combined with CO at the hot end 2 The gas at the top of the absorption tower 15 exchanges heat, the gas at the top of the absorption tower is cooled to 40 ℃, and at the same time, CO is utilized 2 The residual heat at the top of the absorption tower 15 evaporates the liquid refrigerant, heats the gas-phase refrigerant to 65 ℃, enters the second refrigerant expansion generator 10 to generate electricity (power 755 kW), expands the generated gas-phase refrigerant (the temperature is about 43.5 ℃ and the pressure is 1000 kPa), cools the gas-phase refrigerant into a liquid phase (the temperature is about 35 ℃) through the second refrigerant condenser 11, and returns to the second refrigerant storage tank 12, thereby completing the heat exchange-gasification-expansion power generation-condensation cycle of the refrigerant.
The above examples are only illustrative of the preferred embodiments of the present invention and are not intended to limit the scope of the present invention, and various modifications and improvements made by those skilled in the art to the technical solution of the present invention should fall within the scope of protection defined by the claims of the present invention without departing from the spirit of the present invention.
Claims (5)
1. Amine method CO 2 The process medium heat energy recovery combined power generation device in the trapping device is characterized in that: comprises a refrigerant reflux valve group (1), a refrigerant expansion generator I (2), a refrigerant condenser I (3), a refrigerant storage tank I (4), a refrigerant booster pump I (5), a refrigerant distribution valve group (6), an amine liquid regeneration tower waste heat recovery heat exchanger (7) and CO 2 Compressor unit outlet waste heat recovery heat exchanger (8) and CO 2 A refrigeration compressor outlet waste heat recovery heat exchanger (9); the outlet of the refrigerant return valve group (1) is sequentially connected with a refrigerant expansion generator I (2) through a pipeline) The first refrigerant condenser (3), the first refrigerant storage tank (4), the first refrigerant booster pump (5) and the first refrigerant distribution valve group (6) are communicated, the first refrigerant distribution valve group (6) comprises three distribution valves, and the three distribution valves are respectively communicated with the waste heat recovery heat exchanger (7) of the amine liquid regeneration tower and the CO through pipelines 2 Compressor unit outlet waste heat recovery heat exchanger (8) and CO 2 The cold end of the refrigeration compressor outlet waste heat recovery heat exchanger (9) is communicated; waste heat recovery heat exchanger (7) of amine liquid regeneration tower and CO 2 Compressor unit outlet waste heat recovery heat exchanger (8) and CO 2 The hot end outlet of the refrigeration compressor outlet waste heat recovery heat exchanger (9) is respectively communicated with three reflux valves of the refrigerant reflux valve group (1) through pipelines;
the adopted refrigerant is a low boiling point refrigerant;
the top of the amine liquid regeneration tower (18) is sequentially communicated with a hot end inlet of the amine liquid regeneration tower waste heat recovery heat exchanger (7) through a pipeline, a cold end outlet of the amine liquid regeneration tower waste heat recovery heat exchanger (7) is sequentially communicated with the upper part of a regeneration tower top reflux tank (23) through a pipeline, and the bottom of the regeneration tower top reflux tank (23) is sequentially communicated with a regeneration tower top reflux pump (24) and the upper part of the amine liquid regeneration tower (18) through a pipeline;
the top of the regeneration tower top reflux tank (23) is sequentially connected with CO through a pipeline 2 Compressor (22), CO 2 Hot end and CO of compressor unit outlet waste heat recovery heat exchanger (8) 2 Hot side inlet and CO of refrigeration heat exchanger (21) 2 The output pipeline is communicated;
the system also comprises a second refrigerant expansion generator (10), a second refrigerant condenser (11), a second refrigerant storage tank (12), a second refrigerant booster pump (13) and an absorber waste heat recovery heat exchanger (14); the outlet of the second refrigerant expansion generator (10) is sequentially communicated with the second refrigerant condenser (11), the second refrigerant storage tank (12), the second refrigerant booster pump (13), the absorber waste heat recovery heat exchanger (14) and the inlet of the second refrigerant expansion generator (10) through pipelines;
a method of using the cogeneration apparatus comprising the steps of:
amine liquid regenerating tower and compressor waste heat recovery
The refrigerant of 35 ℃ stored in the first refrigerant storage tank (4) is pressurized to 800kPa by the first refrigerant booster pump (5) and then enters into the first refrigerant storage tank respectively:
1) The cold end of the waste heat recovery heat exchanger (7) of the amine liquid regeneration tower and the CO at the top of the amine liquid regeneration tower (18) at the hot end 2 The gas exchanges heat to exchange CO at the top of the tower 2 Cooling the gas to 40 ℃, at the same time, evaporating the liquid refrigerant by utilizing the residual heat of the tower top, and heating the gas-phase refrigerant to 100-102 ℃;
2)CO 2 cold end of refrigerating compressor outlet waste heat recovery heat exchanger (9), and CO 2 High temperature R507 at the outlet of the refrigeration compressor (20) exchanges heat to exchange CO 2 The outlet gas of the refrigeration compressor (20) is cooled to 40 ℃ and at the same time, CO is utilized 2 Evaporating liquid refrigerant by using waste heat at an outlet of a refrigeration compressor (20), and heating the temperature of gas-phase refrigerant to 105 ℃;
3)CO 2 the cold end of the compressor unit outlet waste heat recovery heat exchanger (8) is connected with CO 2 High temperature CO at the compressor (22) outlet 2 Heat exchange is carried out to CO 2 The compressor (22) outlet gas is cooled to 40 ℃ while at the same time utilizing CO 2 Evaporating the liquid refrigerant by using waste heat at the outlet of the compressor (22), and heating the temperature of the gas-phase refrigerant to 115 ℃;
the gas phases of the refrigerants evaporated and vaporized by the three heat exchangers are collected, the temperature is 103-108 ℃, the pressure is 780-3350kPa, the refrigerant enters a first refrigerant expansion generator (2) to generate electricity, the power of generation is 1850-2039kW, the gas phase of the refrigerant after expansion and power generation is 50.7-57 ℃, the pressure is 180-1000kPa, the refrigerant is cooled to be liquid phase by a first refrigerant condenser (3), the temperature is 35 ℃, and the refrigerant flows back to a first refrigerant storage tank (4), so that the heat exchange-gasification-expansion power generation-condensation cycle of the refrigerant is completed;
(II) CO 2 Waste heat recovery of absorption tower (15)
The refrigerant with the temperature of 35 ℃ stored in the second refrigerant storage tank (12) enters the waste heat recovery heat exchanger (14) of the absorption tower after being pressurized by the second refrigerant booster pump (13) by 350-3400kPa, and is communicated with CO at the hot end 2 The gas at the top of the absorption tower (15) exchanges heat, the gas at the top of the absorption tower is cooled to 40 ℃, and at the same time, CO is utilized 2 The top of the absorption tower (15) is remainedThe liquid refrigerant is evaporated by heat, the temperature of the gas-phase refrigerant is heated to 65 ℃, the gas-phase refrigerant enters a second refrigerant expansion generator (10) to generate electricity, the electricity generation power is 700-755kW, the temperature of the gas-phase refrigerant after expansion electricity generation is 43.5-48.4 ℃, the pressure is 160-1000kPa, the gas-phase refrigerant is cooled to be liquid phase by a second refrigerant condenser (11), the temperature is 35 ℃, and the gas-phase refrigerant flows back to a second refrigerant storage tank (12), so that the heat exchange-gasification-expansion electricity generation-condensation cycle of the refrigerant is completed.
2. An amine CO according to claim 1 2 The process medium heat energy recovery combined power generation device in the trapping device is characterized in that: CO 2 The outlet of the refrigeration compressor (20) is sequentially connected with CO through a pipeline 2 Hot end of refrigeration compressor outlet waste heat recovery heat exchanger (9), valve (19), CO 2 Cold side inlet and CO of refrigeration heat exchanger (21) 2 The inlet of the refrigeration compressor (20) is in communication.
3. An amine CO according to claim 1 2 The process medium heat energy recovery combined power generation device in the trapping device is characterized in that: CO 2 The top of the absorption tower (15) is sequentially connected with the waste heat recovery heat exchanger (14) of the absorption tower, the upper part of the reflux tank (16) of the top of the absorption tower and CO through pipelines 2 The upper part of the side wall of the absorption tower (15) is communicated.
4. An amine CO according to claim 3 2 The process medium heat energy recovery combined power generation device in the trapping device is characterized in that: reflux drum (16) and CO at the top of the absorption column 2 An absorption tower top reflux pump (17) is arranged on a pipeline between the absorption towers (15).
5. An amine CO according to any one of claims 1 to 4 2 The process medium heat energy recovery combined power generation device in the trapping device is characterized in that: the low boiling point refrigerant is one of R11 and R134 a.
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Denomination of invention: Process medium heat recovery combined power generation device and method in amine based CO capture device Granted publication date: 20230711 Pledgee: Bank of Nanjing Limited by Share Ltd. Beijing branch Pledgor: Beijing Yuancarbon Environment Co.,Ltd. Registration number: Y2024980012789 |