CN115608118B - Composite absorption tower and absorption type carbon capture pressure increasing system and process - Google Patents
Composite absorption tower and absorption type carbon capture pressure increasing system and process Download PDFInfo
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- CN115608118B CN115608118B CN202211545768.8A CN202211545768A CN115608118B CN 115608118 B CN115608118 B CN 115608118B CN 202211545768 A CN202211545768 A CN 202211545768A CN 115608118 B CN115608118 B CN 115608118B
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- 238000010521 absorption reaction Methods 0.000 title claims abstract description 207
- 239000002131 composite material Substances 0.000 title claims abstract description 52
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 title claims abstract description 32
- 229910052799 carbon Inorganic materials 0.000 title claims abstract description 32
- 238000000034 method Methods 0.000 title claims abstract description 21
- 230000008569 process Effects 0.000 title claims abstract description 20
- 238000001816 cooling Methods 0.000 claims abstract description 80
- 239000007788 liquid Substances 0.000 claims abstract description 75
- 239000002918 waste heat Substances 0.000 claims abstract description 55
- 239000007789 gas Substances 0.000 claims abstract description 53
- 239000011552 falling film Substances 0.000 claims abstract description 37
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 25
- 239000003546 flue gas Substances 0.000 claims abstract description 25
- 239000003507 refrigerant Substances 0.000 claims abstract description 18
- 238000001704 evaporation Methods 0.000 claims abstract description 10
- 230000008020 evaporation Effects 0.000 claims abstract description 10
- 230000005611 electricity Effects 0.000 claims abstract description 9
- 239000010408 film Substances 0.000 claims abstract description 9
- 238000010438 heat treatment Methods 0.000 claims abstract description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 67
- 238000003795 desorption Methods 0.000 claims description 24
- 229920006395 saturated elastomer Polymers 0.000 claims description 24
- 238000000926 separation method Methods 0.000 claims description 21
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 20
- 239000002912 waste gas Substances 0.000 claims description 17
- 239000006096 absorbing agent Substances 0.000 claims description 14
- 150000001875 compounds Chemical class 0.000 claims description 8
- 230000002745 absorbent Effects 0.000 claims description 7
- 239000002250 absorbent Substances 0.000 claims description 7
- 239000000203 mixture Substances 0.000 claims description 7
- 229910021529 ammonia Inorganic materials 0.000 claims description 6
- 239000002699 waste material Substances 0.000 claims description 6
- 238000009834 vaporization Methods 0.000 claims description 4
- 230000008016 vaporization Effects 0.000 claims description 4
- 230000009467 reduction Effects 0.000 claims description 3
- 239000012530 fluid Substances 0.000 claims description 2
- 230000008676 import Effects 0.000 claims 1
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- 238000012986 modification Methods 0.000 description 2
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- 239000012071 phase Substances 0.000 description 2
- 238000005057 refrigeration Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 229910000831 Steel Inorganic materials 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
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- 230000008929 regeneration 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
- B01D53/18—Absorbing units; Liquid distributors therefor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1425—Regeneration of liquid absorbents
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
- B01D53/1475—Removing carbon dioxide
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
- F01D—NON-POSITIVE DISPLACEMENT MACHINES OR ENGINES, e.g. STEAM TURBINES
- F01D15/00—Adaptations of machines or engines for special use; Combinations of engines with devices driven thereby
- F01D15/08—Adaptations for driving, or combinations with, pumps
-
- 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
-
- 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
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
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- General Engineering & Computer Science (AREA)
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Abstract
The invention belongs to the technical field of absorption type carbon capture, and particularly relates to a composite absorption tower, an absorption type carbon capture pressure-raising system and an absorption type carbon capture pressure-raising process, wherein a barren solution cooling section, a liquid collecting film distributor, an in-pipe falling film absorption section and a gas cooling section are sequentially arranged in the composite absorption tower from top to bottom, and the system also comprises two groups of absorption type waste heat power generating units: the turbine generator of the absorption type waste heat generator set is positioned between the generator and the refrigerant pipeline of the condenser, and the turbine generator utilizes high-pressure refrigerant separated out by heating of the generator as driving to generate electricity. The invention uses the heat contained in the low-pressure flue gas and the low-pressure steam to drive the absorption type waste heat generator set, the electricity generated by the absorption type waste heat generator set is used for driving the fan and the solution pump, and meanwhile, the evaporation cooling end in the absorption type waste heat generator set is used for cooling the absorption section of the absorption tower. The utilization rate of the energy in the unit is improved, and the energy consumption of the unit is reduced.
Description
Technical Field
The invention belongs to the technical field of absorption type carbon capture, and particularly relates to a composite absorption tower, an absorption type carbon capture pressure increasing system and an absorption type carbon capture pressure increasing process.
Background
At present, the absorption-type carbon capture pressure-increasing system can be used for capturing and recovering CO in mixed gas such as chemical tail gas, power plant gas tail gas, cement roasting flue gas and the like 2 And can be used directly for CO 2 And (5) increasing the pressure. As shown in FIG. 1, contains CO 2 The low-pressure flue gas is pressurized by a fan, enters a gas cooler for cooling, is sent to an absorption tower to contact with an absorbent from the top of the tower in a packing layer for absorbing CO 2 Purified tail gasDischarging the liquid from the top of the tower, pumping the rich liquid from the bottom of the tower, heating in lean-rich heat exchanger, and feeding the rich liquid to the desorption tower, wherein the rich liquid flows from top to bottom in the desorption tower and the CO is pyrolyzed and sucked out by the reboiler 2 The mixture with the water vapor flows from bottom to top to carry out countercurrent contact heat and mass transfer in the packing layer to finish CO 2 Desorption and regeneration of the absorbent. The barren solution desorbed in the desorption tower flows out from the bottom of the tower, sequentially passes through the barren and rich heat exchanger and the barren solution cooler for cooling, is decompressed by the decompression valve, and then enters the absorption tower. CO desorbed from the desorption tower 2 The mixture with water vapor flows out from the top of the tower, enters a condenser for condensation, then enters a gas-liquid separation tank, and separated high-pressure CO 2 In the subsequent working section, CO 2 The separated water flows back to the desorption tower. The heat required by heating and desorption in the reboiler is obtained by reducing the temperature and pressure of low-pressure steam. The absorption process is used for carbon capture and CO capture in the industrial fields of chemical industry, cement, steel, natural gas, coal power and the like 2 The equipment investment and the operation cost can be obviously reduced in the hot pressure raising process, and the method has high economic value and social value.
The above process has many spaces for process optimization and equipment integration. For example, the heat contained in the low-pressure flue gas is not utilized before entering the fan, and the power consumption of the fan is increased by compressing and boosting the high-temperature flue gas. The low-pressure steam passes through a temperature and pressure reducing device before entering the reboiler, and part of heat energy is not utilized.
The absorbent that flows from the top down in the absorption tower and the flue gas that rises from the bottom up carry out countercurrent contact absorption in the packing layer, have the heat to emit among the absorption process, lead to the temperature of absorbent to rise to can reduce the absorption efficiency of absorption tower, lead to the tower body packing layer to increase, increase the investment of equipment.
Disclosure of Invention
In order to solve the problems mentioned in the background technology, a composite absorption tower, an absorption type carbon capture pressure increasing system and a process are provided.
The purpose is achieved through the following technical scheme:
the invention provides a composite absorption tower, which comprises a tower body, and a waste gas inlet, a purified gas outlet, a rich liquid outlet and a barren liquid inlet which are arranged on the tower body,
the device is characterized in that a barren solution cooling section, a liquid collecting and film distributing device, an in-pipe falling film absorption section and a gas cooling section are sequentially arranged in the tower body from top to bottom, and the barren solution cooling section, the in-pipe falling film absorption section and the gas cooling section are all formed by fixed pipe plate type pipe bundles; the lean solution inlet is positioned above the lean solution cooling section, and the waste gas inlet is positioned below the gas cooling section;
circulating water in the barren liquor cooling section and barren liquor heat transfer back through the tower body outside one-way pipe let in between intraductal falling film absorption section and the gas cooling section regional, circulating water in the gas cooling section and contain behind the heat transfer of hot waste gas through the tower body outside one-way pipe let in between intraductal falling film absorption section and the gas cooling section regional.
As a further improvement of the technical scheme, the fixed tube sheet type tube bundle comprises an upper tube sheet, a lower tube sheet, a heat exchange tube positioned between the upper tube sheet and the lower tube sheet and a baffle plate for fixing the heat exchange tube.
As a further improvement of the technical scheme, the heat exchange tube fluids of the barren liquor cooling section, the in-tube falling film absorption section and the gas cooling section are all in a countercurrent upward state.
As a further improvement of the technical scheme, a one-way valve is arranged on the one-way pipeline outside the tower body.
The invention also provides an absorption type carbon capture pressure boosting system which comprises a solution pump, a lean-rich liquid heat exchanger, a desorption tower, a cooler, a gas-liquid separation tank and a reboiler, and also comprises the composite absorption tower and two groups of absorption type waste heat generator sets;
the absorption type waste heat generator set comprises a generator, a turbine generator, a condenser, a GVX heat exchanger, an absorber, a precooler and a GAX heat exchanger, wherein the turbine generator is positioned between a generator and a refrigerant pipeline of the condenser, and the turbine generator utilizes a high-pressure refrigerant separated out by heating of the generator as a drive to generate electricity;
the generator of one group of absorption type waste heat generator sets takes waste gas as a heat source, the waste gas after heat exchange is connected with a waste gas inlet of the composite absorption tower through a fan, and a turbine generator in the absorption type waste heat generator sets supplies power to the fan; the generator of the other group of absorption type waste heat generator sets takes waste steam as a heat source, the waste steam after heat exchange forms condensate through a reboiler, and a turbine generator in the absorption type waste heat generator sets supplies power to a solution pump between the composite absorption tower and the lean-rich liquid heat exchanger.
As a further improvement of the above technical scheme, in the two groups of absorption type waste heat power generator sets, the GVX heat exchangers are located between the condenser and the absorber, and the liquid refrigerant of the condenser enters the GVX heat exchangers and then enters the in-tube falling film absorption section of the composite absorption tower, and then returns to the GVX heat exchangers and then enters the absorber.
As a further improvement of the technical scheme, a liquid outlet of the gas-liquid separation tank is divided into two paths through a pressure reducing valve, one path is connected to a barren solution cooling section of the composite absorption tower, and the other path is connected to a gas cooling section of the composite absorption tower.
The invention also provides an absorption type carbon capture pressure-raising process which is realized by utilizing the absorption type carbon capture pressure-raising system, low-pressure flue gas and low-pressure steam are respectively introduced into two groups of absorption type waste heat generator sets, electricity generated by the absorption type waste heat generator sets is respectively used for driving a fan and a solution pump, and meanwhile, an in-pipe falling film absorption section of the composite absorption tower is used as an evaporation cooling end in the absorption type waste heat generator sets;
the process comprises the following steps:
(1) Establishing circulation of an absorption type waste heat generator set: a refrigerant flow for communicating a condenser, a composite absorption tower, an absorber and a generator is adopted, low-pressure flue gas and low-pressure steam are respectively introduced into generators of two groups of absorption type waste heat generator sets, the desorbed high-pressure refrigerant drives a turbine generator set and then enters the condenser, meanwhile, low-pressure liquid ammonia entering the GVX heat exchanger of the condenser is introduced into a falling film absorption section of the absorption tower for cooling the composite absorption tower in the process of absorbing the flue gas, and the gas ammonia after heat absorption and vaporization returns to the absorption type waste heat generator set for circulating operation;
(2) Establishing an absorption carbon capture cycle: working medium liquid circulation flow for communicating composite absorption tower, desorption tower, cooler and gas-liquid separation tank and containing CO 2 The low-pressure flue gas enters an absorption tower and is mixed with an absorbent to form a rich solution, the rich solution enters a desorption tower, and CO desorbed from the desorption tower 2 The mixture with water vapor flows out of the tower top and enters a cooler to be condensed into liquid water and gaseous CO 2 Then the mixture enters a gas-liquid separation tank for separation, and CO at the top part 2 And the water is discharged from the upper part, the water at the bottom is refluxed into low-pressure saturated water after throttling and pressure reduction, the low-pressure saturated water is divided into two paths, one path of the low-pressure saturated water enters a lean liquid cooling section of the composite absorption tower to absorb the heat of the lean liquid and evaporate into water vapor, the other path of the low-pressure saturated water enters a gas cooling section of the composite absorption tower to absorb the heat of the gas and evaporate into the water vapor, the two paths of the low-pressure saturated water absorb the heat and evaporate into the water vapor, the water vapor is introduced into the composite absorption tower to be absorbed, and the low-pressure saturated water returns to the working medium liquid of the carbon capture system to continue to operate circularly.
The invention has the beneficial effects that:
(1) The composite absorption tower integrates the gas cooler, the barren liquor cooler and the absorption tower, so that the cost of a unit pipeline can be reduced, and the occupied area of the unit is greatly reduced. Meanwhile, a mode of in-pipe falling film absorption and outside-pipe liquid ammonia evaporation heat transfer is used for replacing a packing layer. The absorption efficiency of the absorption tower is greatly improved, and the carbon capture performance of the unit is improved.
(2) The heat contained in the low-pressure flue gas and the low-pressure steam is used for driving the absorption type waste heat generator set, the electricity generated by the absorption type waste heat generator set is used for driving the fan and the solution pump, and meanwhile, the evaporation refrigerating end in the absorption type waste heat generator set is used for cooling the absorption section of the absorption tower. The utilization rate of the energy in the unit is improved, and the energy consumption of the unit is reduced.
(3) The water separated and refluxed from the gas-liquid separation tank at the top of the desorption tower is throttled and decompressed to form low-pressure saturated water, the low-pressure saturated water is introduced into a gas cooler and a barren solution cooler and used for cooling the flue gas and the barren solution, and the low-pressure saturated water absorbs heat and is evaporated into water vapor which is introduced into an absorption tower to be absorbed and then returns to the rich solution again. The evaporation heat absorption with phase change replaces pure liquid phase water cooling in the original system, so that the consumption of circulating water in the system can be greatly saved, the load of a cooling tower is reduced, and the power consumption is reduced.
Drawings
FIG. 1 is a schematic diagram of a prior art carbon capture pressure increasing system;
FIG. 2 is a schematic diagram of a prior art absorption tower configuration;
FIG. 3 is a schematic view of a composite absorption tower according to the present invention;
FIG. 4 is a schematic flow diagram of an absorption carbon capture pressure boosting system of the present invention;
FIG. 5 is a schematic flow diagram of an absorption carbon capture pressure letup train of the present invention;
fig. 6 is a schematic flow diagram of an absorption waste heat generator set of the present invention.
The figure is as follows: 100. an exhaust gas inlet; 200. a purified gas outlet; 300. a rich liquid outlet; 400. a barren liquor inlet; 500. a lean solution cooling section; 600. a liquid collecting and film distributing device; 700. an in-tube falling film absorption section; 800. a gas cooling section; 900. a one-way valve;
1. a composite absorption tower; 2. a fan; 3. a solution pump; 4. a lean-rich liquid heat exchanger; 5. a desorption tower; 6. a cooler; 7. a gas-liquid separation tank; 8. a reboiler; 9. an absorption type waste heat generator set; 91. a generator; 92. a turbine generator; 93. a condenser; 94. a GVX heat exchanger; 95. an absorber; 96. a precooler; 97. and a GAX heat exchanger.
Detailed Description
The present application will now be described in further detail with reference to the drawings, and it should be noted that the following detailed description is given for purposes of illustration only and should not be construed as limiting the scope of the present application, as these numerous non-limiting modifications and variations will suggest themselves to those skilled in the art in light of the foregoing disclosure.
As shown in fig. 3, the composite absorption tower 1 of the present embodiment includes a tower body, and a waste gas inlet 100, a purified gas outlet 200, a rich liquid outlet 300, and a lean liquid inlet 400 on the tower body,
the interior of the tower body is sequentially provided with a barren solution cooling section 500, a liquid collecting and film distributing device 600, an in-pipe falling film absorption section 700 and a gas cooling section 800 from top to bottom, and the barren solution cooling section 500, the in-pipe falling film absorption section 700 and the gas cooling section 800 are all formed by fixed pipe plate type pipe bundles; the lean liquid inlet 400 is located above the lean liquid cooling section 500, and the exhaust gas inlet 100 is located below the gas cooling section 800;
circulating water in the lean solution cooling section 500 exchanges heat with lean solution and then is introduced into the area between the in-pipe falling film absorption section 700 and the gas cooling section 800 through a one-way pipeline outside the tower body, and circulating water in the gas cooling section 800 exchanges heat with hot waste gas and then is introduced into the area between the in-pipe falling film absorption section 700 and the gas cooling section 800 through a one-way pipeline outside the tower body.
The fixed tube sheet type tube bundle comprises an upper tube sheet, a lower tube sheet, a heat exchange tube positioned between the upper tube sheet and the lower tube sheet and a baffle plate for fixing the heat exchange tube, and a shell of the compound absorption tower 1 forms a shell pass of the fixed tube sheet type tube bundle.
Compared with the absorption tower shown in fig. 2, in the composite absorption tower 1 of the embodiment, the heat exchange tube side of the lean liquid cooling section 500 is filled with the lean liquid, from top to bottom, the shell side of the lean liquid cooling section 500 is filled with the low-pressure saturated water (which is formed by throttling and reducing the pressure of the water separated and refluxed from the gas-liquid separation tank 7 at the top of the desorption tower 5 through the pressure reducing valve), the low-pressure saturated water and the lean liquid are operated in a countercurrent mode, the heat of the absorbed lean liquid is evaporated into steam, and the steam is introduced into the lower end of the in-tube falling film absorption section 700 through the check valve 900 and enters the in-tube falling film absorption section 700 to be absorbed. The barren liquor flowing down from the tube pass in the barren liquor cooling section 500 is subjected to film distribution in the tube falling film absorption section 700 through the liquid collecting and film distributing device 600 to form a liquid film flowing down along the tube wall, and the flue gas and the water vapor from the barren liquor cooling section 500 and the gas cooling section 800 are subjected to countercurrent operation with the liquid film from bottom to top in the tube falling film absorption section 700 to be in contact absorption. The absorbed and released heat is evaporated and taken away by low-pressure liquid ammonia in the shell pass of the in-tube falling film absorption section 700 (the low-pressure liquid ammonia is from the absorption type waste heat power generator set 9). The gas cooling section 800 is used for flowing flue gas on the tube pass, from bottom to top, the gas cooling section 800 is used for flowing low-pressure saturated water (formed by throttling and decompressing water separated and refluxed from a gas-liquid separation tank 7 at the top of the desorption tower 5 through a pressure reducing valve) on the shell pass, the low-pressure saturated water absorbs heat of the flue gas and evaporates into water vapor, and then the water vapor is introduced into the lower end of the falling film absorption section 700 in the tube through a one-way valve 900 and enters the falling film absorption section 700 in the tube to be absorbed.
Applied to an absorption type carbon capture pressure-increasing system, compared with the figure 1, the barren liquor cooling section 500 replaces a barren liquor cooler, the falling film absorption section 700 in the pipe replaces a packing layer and is equivalent to an evaporator in the absorption type waste heat power generator set 9, and the body cooling section replaces a gas cooler.
As shown in fig. 4, the absorption carbon capture pressure raising system in this embodiment includes a solution pump 3, a lean-rich liquid heat exchanger 4, a desorption tower 5, a cooler 6, a gas-liquid separation tank 7, a reboiler 8, the composite absorption tower 1, and two sets of absorption waste heat power generators 9;
as shown in fig. 5, the absorption-type waste heat generator set 9 includes a generator 91, a turbine generator 92, a condenser 93, a GVX heat exchanger 94, an absorber 95, a precooler 96 and a GAX heat exchanger 97, the turbine generator 92 is located between refrigerant pipelines of the generator 91 and the condenser 93, and the turbine generator 92 is driven by high-pressure refrigerant separated by the generator 91 after being heated to generate electricity; the generator 91 of one group of the absorption type waste heat generator set 9 takes waste gas as a heat source, the waste gas after heat exchange is connected with a waste gas inlet 100 of the composite absorption tower 1 through a fan 2, and a turbine generator 92 in the absorption type waste heat generator set 9 supplies power to the fan 2; the generator 91 of the other group of absorption type waste heat generator set 9 uses waste steam as a heat source, the waste steam after heat exchange passes through the reboiler 8 to form a condensate, and the turbine generator 92 in the absorption type waste heat generator set 9 supplies power to the solution pump 3 between the compound absorption tower 1 and the lean and rich liquid heat exchanger 4.
The absorption-type waste heat generator set 9 is an improvement on an ammonia absorption-type refrigerating unit, a turbine generator 92 is added between a generator 91 and a condenser 93, and high-pressure refrigerant ammonia desorbed from the generator 91 drives the turbine generator 92 and then enters the condenser 93. Meanwhile, liquid ammonia in a low-pressure state at an evaporation refrigeration end is introduced into a falling film absorption section of the absorption tower 1 to be used for cooling in the absorption process, and gas ammonia after heat absorption and vaporization returns to the absorption type waste heat generator set 9 to operate circularly.
In the two groups of absorption type waste heat generator sets 9, the GVX heat exchanger 94 is located between the condenser 93 and the absorber 95, the liquid refrigerant of the condenser 93 enters the GVX heat exchanger 94 and then enters the in-tube falling film absorption section 700 of the compound absorption tower 1, and then returns to the GVX heat exchanger 94 and then enters the absorber 95, the in-tube falling film absorption section 700 in the compound absorption tower 1 is used as the evaporator of the two groups of absorption type waste heat generator sets 9, and the low-pressure liquid ammonia at the evaporation and refrigeration end of the absorption type waste heat generator sets 9 is introduced into the in-tube falling film absorption section 700 in the compound absorption tower 1 for cooling the flue gas absorption process.
The liquid outlet of the gas-liquid separation tank 7 is divided into two paths by a pressure reducing valve, one path is connected to the lean liquid cooling section 500 of the composite absorption tower 1, and the other path is connected to the gas cooling section 800 of the composite absorption tower 1. The water separated and refluxed in the gas-liquid separation tank 7 at the top of the desorption tower 5 is throttled and decompressed by a pressure reducing valve to form low-pressure saturated water, the low-pressure saturated water is introduced into a gas cooling section 800 and a barren solution cooling section 500 in the composite absorption tower 1 to be used for cooling the flue gas and the barren solution, and the low-pressure saturated water absorbs heat and evaporates to form water vapor which is introduced into the composite absorption tower 1 to be absorbed and returns to the rich solution again. The evaporation heat absorption with phase change replaces pure liquid phase water cooling in the original system, so that the consumption of circulating water in the system can be greatly saved, the load of a cooling tower is reduced, and the power consumption is reduced.
In the absorption carbon capture pressure-raising process in the embodiment, low-pressure flue gas and low-pressure steam are respectively introduced into two groups of absorption waste heat power generating units, electricity generated by the absorption waste heat power generating units is respectively used for driving a fan 2 and a solution pump 3, and meanwhile, an in-pipe falling film absorption section 700 of the composite absorption tower 1 is used as an evaporation cooling end in the absorption waste heat power generating units;
the process comprises the following steps:
(1) Establishing 9 cycles of an absorption type waste heat generator set: a refrigerant flow path for communicating the condenser 93 with the compound absorption tower 1, the absorber 95 with the generator 91 is characterized in that low-pressure flue gas and low-pressure steam are respectively introduced into the generator 91 of the two groups of absorption type waste heat generator sets 9, the desorbed high-pressure refrigerant drives the turbine generator 92 group and then enters the condenser 93, meanwhile, liquid ammonia in a low-pressure state, which enters the GVX heat exchanger 94 from the condenser 93, is introduced into a falling film absorption section of the absorption tower 1 for cooling the compound absorption tower 1 in the process of absorbing the flue gas, and the gas ammonia after heat absorption and vaporization returns to the absorption type waste heat generator sets 9 for circulating operation;
(2) Establishing an absorption carbon capture cycle: working medium liquid circulation flow for communicating the composite absorption tower 1-the desorption tower 5-the cooler 6-the gas-liquid separation tank 7 and containing CO 2 The low-pressure flue gas enters the absorption tower 1 and CO 2 The absorbent is mixed to form rich liquid which enters a desorption tower 5, and CO desorbed from the desorption tower 5 2 The mixture with water vapor flows out of the tower top into a cooler 6 to be condensed into liquid water and gaseous CO 2 Then enters a gas-liquid separation tank 7 for separation, and CO at the top part 2 And (3) discharging from the upper part, wherein water at the bottom is refluxed into low-pressure saturated water after throttling and pressure reduction and then is divided into two paths, one path of water enters a lean liquid cooling section 500 of the composite absorption tower 1 to absorb heat of the lean liquid to be evaporated into steam, the other path of water enters a gas cooling section 800 of the composite absorption tower 1 to absorb heat of gas to be evaporated into steam, the two paths of low-pressure saturated water absorb heat to be evaporated into steam, the steam is introduced into the composite absorption tower 1 to be absorbed, and the steam returns to the working medium liquid of the carbon capture system to continue to operate circularly.
The above-mentioned embodiments only express several embodiments of the present invention, and the description thereof is specific and detailed, but not to be understood as limiting the scope of the present invention. It should be noted that, for a person skilled in the art, several modifications can be made without departing from the inventive concept, which falls within the scope of the present invention.
Claims (8)
1. The utility model provides a compound absorption tower, includes the tower body and is located waste gas air inlet, purification gas outlet, rich liquid export, barren liquor import on the tower body which characterized in that:
the device is characterized in that a barren solution cooling section, a liquid collecting and film distributing device, an in-pipe falling film absorption section and a gas cooling section are sequentially arranged in the tower body from top to bottom, and the barren solution cooling section, the in-pipe falling film absorption section and the gas cooling section are all formed by fixed pipe plate type pipe bundles; the lean solution inlet is positioned above the lean solution cooling section, and the waste gas inlet is positioned below the gas cooling section;
circulating water in the barren liquor cooling section and barren liquor heat transfer back let in between intraductal falling film absorption section and the gas cooling section through the outer one-way pipe of tower body, circulating water in the gas cooling section and contain behind the heat transfer of hot waste gas let in between intraductal falling film absorption section and the gas cooling section through the outer one-way pipe of tower body.
2. A composite absorber tower as claimed in claim 1, wherein the fixed tube sheet bundle comprises upper and lower tube sheets, heat exchange tubes between the upper and lower tube sheets, and baffles for securing the heat exchange tubes.
3. The composite absorption tower according to claim 1, wherein the heat exchange pipe fluid of the barren liquid cooling section, the in-pipe falling film absorption section and the gas cooling section is in a countercurrent upward state.
4. The composite absorption tower of claim 1, wherein a check valve is disposed on the check pipe outside the tower body.
5. An absorption type carbon capture pressure-raising system comprises a solution pump, a lean-rich liquid heat exchanger, a desorption tower, a cooler, a gas-liquid separation tank and a reboiler, and is characterized by further comprising a composite absorption tower as claimed in any one of claims 1 to 4 and two groups of absorption type waste heat generator sets;
the absorption type waste heat generator set comprises a generator, a turbine generator, a condenser, a GVX heat exchanger, an absorber, a precooler and a GAX heat exchanger, wherein the turbine generator is positioned between a generator and a refrigerant pipeline of the condenser, and the turbine generator utilizes high-pressure refrigerant separated out by heating of the generator as drive to generate electricity;
the generator of one group of absorption type waste heat generator sets takes waste gas as a heat source, the waste gas after heat exchange is connected with a waste gas inlet of the composite absorption tower through a fan, and a turbine generator in the absorption type waste heat generator sets supplies power to the fan; the generator of the other group of absorption type waste heat generator sets takes waste steam as a heat source, the waste steam after heat exchange forms condensate through a reboiler, and a turbine generator in the absorption type waste heat generator sets supplies power to a solution pump between the composite absorption tower and the lean-rich liquid heat exchanger.
6. The absorption carbon capture pressure boosting system according to claim 5, wherein in the two groups of absorption waste heat power generator sets, the GVX heat exchanger is positioned between the condenser and the absorber, and liquid refrigerant of the condenser enters the GVX heat exchanger and then enters the in-pipe falling film absorption section of the composite absorption tower, returns to the GVX heat exchanger and then enters the absorber.
7. The absorption-type carbon capture pressure boosting system according to claim 5, wherein a liquid outlet of the gas-liquid separation tank is divided into two paths by a pressure reducing valve, one path is connected to a lean liquid cooling section of the composite absorption tower, and the other path is connected to a gas cooling section of the composite absorption tower.
8. An absorption type carbon capture pressure-raising process is realized by using the absorption type carbon capture pressure-raising system of any one of claims 5 to 7, low-pressure flue gas and low-pressure steam are respectively introduced into two groups of absorption type waste heat power generating units, electricity generated by the absorption type waste heat power generating units is respectively used for driving a fan and a solution pump, and meanwhile, an in-pipe falling film absorption section of the composite absorption tower is used as an evaporation cooling end in the absorption type waste heat power generating units;
the process comprises the following steps:
(1) Establishing circulation of an absorption type waste heat generator set: a refrigerant flow for communicating a condenser, a composite absorption tower, an absorber and a generator is adopted, low-pressure flue gas and low-pressure steam are respectively introduced into generators of two groups of absorption type waste heat generator sets, the desorbed high-pressure refrigerant drives a turbine generator set and then enters the condenser, meanwhile, low-pressure liquid ammonia entering the GVX heat exchanger of the condenser is introduced into a falling film absorption section of the absorption tower for cooling the composite absorption tower in the process of absorbing the flue gas, and the gas ammonia after heat absorption and vaporization returns to the absorption type waste heat generator set for circulating operation;
(2) Establishing an absorption carbon capture cycle: working medium liquid circulation flow for communicating composite absorption tower, desorption tower, cooler and gas-liquid separation tank and containing CO 2 The low-pressure flue gas enters an absorption tower and is mixed with an absorbent to form a rich solution, the rich solution enters a desorption tower, and CO desorbed from the desorption tower 2 The mixture with water vapor flows out of the tower top and enters a cooler to be condensed into liquid water and gaseous CO 2 Then the mixture enters a gas-liquid separation tank for separation, and CO at the top part 2 And the water is discharged from the upper part, the water at the bottom is refluxed into low-pressure saturated water after throttling and pressure reduction, the low-pressure saturated water is divided into two paths, one path of the low-pressure saturated water enters a lean liquid cooling section of the composite absorption tower to absorb the heat of the lean liquid and evaporate into water vapor, the other path of the low-pressure saturated water enters a gas cooling section of the composite absorption tower to absorb the heat of the gas and evaporate into the water vapor, the two paths of the low-pressure saturated water absorb the heat and evaporate into the water vapor, the water vapor is introduced into the composite absorption tower to be absorbed, and the low-pressure saturated water returns to the working medium liquid of the carbon capture system to continue to operate circularly.
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