CN116951803A - CO 2 Heat pump driven direct air carbon capture system with recirculation purging and method thereof - Google Patents
CO 2 Heat pump driven direct air carbon capture system with recirculation purging and method thereof Download PDFInfo
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- CN116951803A CN116951803A CN202310897457.6A CN202310897457A CN116951803A CN 116951803 A CN116951803 A CN 116951803A CN 202310897457 A CN202310897457 A CN 202310897457A CN 116951803 A CN116951803 A CN 116951803A
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- 238000010438 heat treatment Methods 0.000 claims description 13
- 239000002918 waste heat Substances 0.000 claims description 9
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 5
- 229910002091 carbon monoxide Inorganic materials 0.000 claims description 3
- 230000008878 coupling Effects 0.000 claims description 3
- 238000010168 coupling process Methods 0.000 claims description 3
- 238000005859 coupling reaction Methods 0.000 claims description 3
- 238000005265 energy consumption Methods 0.000 abstract description 23
- 238000004064 recycling Methods 0.000 abstract description 10
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 128
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- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 description 1
- OHVLMTFVQDZYHP-UHFFFAOYSA-N 1-(2,4,6,7-tetrahydrotriazolo[4,5-c]pyridin-5-yl)-2-[4-[2-[[3-(trifluoromethoxy)phenyl]methylamino]pyrimidin-5-yl]piperazin-1-yl]ethanone Chemical compound N1N=NC=2CN(CCC=21)C(CN1CCN(CC1)C=1C=NC(=NC=1)NCC1=CC(=CC=C1)OC(F)(F)F)=O OHVLMTFVQDZYHP-UHFFFAOYSA-N 0.000 description 1
- LDXJRKWFNNFDSA-UHFFFAOYSA-N 2-(2,4,6,7-tetrahydrotriazolo[4,5-c]pyridin-5-yl)-1-[4-[2-[[3-(trifluoromethoxy)phenyl]methylamino]pyrimidin-5-yl]piperazin-1-yl]ethanone Chemical compound C1CN(CC2=NNN=C21)CC(=O)N3CCN(CC3)C4=CN=C(N=C4)NCC5=CC(=CC=C5)OC(F)(F)F LDXJRKWFNNFDSA-UHFFFAOYSA-N 0.000 description 1
- JQMFQLVAJGZSQS-UHFFFAOYSA-N 2-[4-[2-(2,3-dihydro-1H-inden-2-ylamino)pyrimidin-5-yl]piperazin-1-yl]-N-(2-oxo-3H-1,3-benzoxazol-6-yl)acetamide Chemical compound C1C(CC2=CC=CC=C12)NC1=NC=C(C=N1)N1CCN(CC1)CC(=O)NC1=CC2=C(NC(O2)=O)C=C1 JQMFQLVAJGZSQS-UHFFFAOYSA-N 0.000 description 1
- YLZOPXRUQYQQID-UHFFFAOYSA-N 3-(2,4,6,7-tetrahydrotriazolo[4,5-c]pyridin-5-yl)-1-[4-[2-[[3-(trifluoromethoxy)phenyl]methylamino]pyrimidin-5-yl]piperazin-1-yl]propan-1-one Chemical compound N1N=NC=2CN(CCC=21)CCC(=O)N1CCN(CC1)C=1C=NC(=NC=1)NCC1=CC(=CC=C1)OC(F)(F)F YLZOPXRUQYQQID-UHFFFAOYSA-N 0.000 description 1
- 239000002028 Biomass Substances 0.000 description 1
- AFCARXCZXQIEQB-UHFFFAOYSA-N N-[3-oxo-3-(2,4,6,7-tetrahydrotriazolo[4,5-c]pyridin-5-yl)propyl]-2-[[3-(trifluoromethoxy)phenyl]methylamino]pyrimidine-5-carboxamide Chemical compound O=C(CCNC(=O)C=1C=NC(=NC=1)NCC1=CC(=CC=C1)OC(F)(F)F)N1CC2=C(CC1)NN=N2 AFCARXCZXQIEQB-UHFFFAOYSA-N 0.000 description 1
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Classifications
-
- 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
-
- 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
- F25B41/00—Fluid-circulation arrangements
- F25B41/40—Fluid line arrangements
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- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Separation Of Gases By Adsorption (AREA)
Abstract
The invention discloses a CO 2 The heat pump driving direct air carbon capturing system with the recycling purging comprises a heat pump subsystem and a direct air carbon capturing subsystem, wherein a heat pump evaporator of the heat pump subsystem provides cold energy for a first condenser used for condensing produced gas in the direct air carbon capturing subsystem; partial high pressure CO generated by the direct air carbon capture subsystem 2 And the gas is heated by a heat pump condenser of the heat pump subsystem to provide desorption heat for an adsorption tower of the direct air carbon capture subsystem. The invention utilizes the condenser and the evaporator of the heat pump as recycle CO respectively 2 Purge gas and H in produced gas 2 The condensation of O provides heat and cold energy, so that an efficient energy supply mode is realized, the comprehensive energy consumption of the whole DAC for capturing, separating and purifying is greatly reduced, and the comprehensive energy utilization efficiency of the system is effectively improved.
Description
Technical Field
The invention relates to a direct air carbon capture device, in particular to a CO 2 A recirculating purged heat pump drives a direct air carbon capture system and method.
Background
Global warming is becoming an increasingly serious problem, and fossil fuels remain the dominant energy source in the world today, which also results in global annual total CO 2 The discharge amount reached about 35Gt. The climate change Integrated Assessment (IAM) model showed that to ensure that the global average temperature rise was kept within 2℃at the end of the 21 st century, CO was maintained by 2050 2 The trapping rate should reach 5-23 Gt/yr and 8-50 Gt/yr by 2100 years. To achieve a more stringent 1.5 ℃ temperature rise target, even cumulative CO is required 2 Negative emission technique with trapping amount of 400-800 Gt.
While lower cost carbon capture can be achieved from conventional power plants and industrial flue gas point emissions sources, some plants are too old to be retrofitted with this technology. Furthermore, the average CO of the power plant 2 The trapping rate is between 50 and 94 percent, so that a part of CO still exists 2 Venting to atmosphere. On the other hand, the mobile emission source in the traffic field is hardly equipped with the carbon capture apparatus, and this part of the emission amount accounts for about 50% of the total emission amount. Therefore, there is a need to develop a carbon capture device independent of the emission source that captures CO directly from the air 2 . The CO of the air can be reduced by adopting negative emission technologies such as biomass carbon trapping and sealing (bioenergy with carbon capture and storage, BECCS), forestation, enhanced weathering, biochar, ocean enrichment, soil carbon fixation and the like 2 Concentration, however, these techniques present themselves with different risks, for example, large scale BECCS and forestation require large amounts of land to threaten biodiversity, and enhanced weathering may cause changes in river, ocean ph and chemical composition.
Direct air capture (Direct Air Capture, DAC) refers to the extraction of CO from the atmosphere by absorption or adsorption 2 . DAC based on absorption/adsorption and subsequent sequestration or utilization provides an effective negative emission path useful for removal of CO from air 2 Reduces the negative impact of fossil fuel usage and creates a closed carbon cycle. DAC technology was originally used for air prepurification and containment of trace CO in space division devices (e.g., submarines and spacecraft) 2 And (5) removing. Currently, DAC application in the negative emission field has become a research hotspot.
As a technology related to materials, circulation and systems, research on DAC is currently mainly focused on the preparation of high-performance adsorbents, design of efficient adsorption and desorption circulation modes, development of efficient traps, and the like. In the preparation of high performance adsorbents, amine functionalized sorbents have been formedA large group of CO with different properties represented by the attachment agent 2 Adsorbents, including inorganic, organic amine, ion exchange resin, and emerging MOF, COF, etc., are characterized by high performance, namely high CO 2 Equilibrium adsorption quantity, rapid adsorption reaction kinetics, good adsorption selectivity (CO 2 /H 2 O,CO 2 /N 2 Adsorption selectivity), excellent cycle stability, lower desorption energy consumption, and the like. In terms of efficient adsorption and desorption cycle design, various cycles have been developed for DAC applications, including TSA (Temperature Swing Adsorption, temperature swing cycle), TVSA (Temperature Vacuum Swing Adsorption, temperature swing vacuum cycle), TCSA (Temperature Concentration Swing Adsorption, temperature swing concentration cycle), and steam, inert gas or CO 2 A cyclic manner of auxiliary desorption. The main differences between the above-mentioned circulation modes are the conditions required to achieve adsorption and desorption and the difference in product gas concentration. For example, the TVSA cycle has a relatively lower desorption temperature due to the increased vacuum compared to the TSA cycle; the inert gas TCSA circulation adopts a gas purging mode to improve desorption rate and circulation efficiency, but simultaneously reduces CO in the product gas 2 Is a concentration of (2); steam purging may separate H through a subsequent condensing step 2 O, but at the same time increases the condensing energy consumption required for water condensation. In contrast, high concentration CO is used 2 The gas recycling purging mode can obtain higher CO without increasing the energy consumption of additional water condensation 2 The gas production concentration is therefore considered a promising DAC cycling regime.
The main problem with current DAC technology is the high capture power consumption. Compared with 2-4 GJ/t of flue gas trapping, the DAC always needs 6-8 GJ/t or even higher trapping energy consumption, and commercial operation and large-scale arrangement of the DAC are severely limited. In addition to developing good adsorption selectivity and low desorption energy consumption adsorbents, building a heat pump driven DAC system is an emerging technology for reducing DAC capture energy consumption. Through searching, patent document CN115077130B discloses a double-heat source heat pump type air carbon direct capturing system,comprises a waste heat recovery system, a high-temperature heat supply heat pump system and air CO 2 A continuous direct capture system; air CO 2 The heat exchange fluid in the carbon adsorption subsystem and the carbon desorption subsystem in the continuous direct trapping system is the refrigerant of the high-temperature heat supply heat pump system; in the high-temperature heat supply heat pump system, waste heat recovered by the waste heat recovery system and adsorption heat generated by the carbon adsorption subsystem form a double heat source for providing heat required by the carbon desorption subsystem, so that the energy consumption of the system is effectively reduced. Patent document CN115479406a discloses a carbon-absorbing air source heat pump composite system, comprising a double-carbon tower and a heat pump; the solution tank of the carbon absorption tower is filled with absorbable CO 2 The solution outlet is pumped to a heat pump evaporator through the solution pump, and the heat of a heat pump condenser is used for building heating; the system has the functions of carbon capture and heat recovery, reduces building heating energy consumption, and increases the economic benefit of integral circulation. From the above patent documents, it can be seen that the conventional heat pump driving DAC system has the following problems: 1) The heat pump and the DAC are only coupled through heat, and the problem of cold energy matching between the heat pump and the DAC is not yet researched, but is the key point for constructing a high-efficiency heat pump driving DAC system; 2) DAC adsorption tower relates to CO in air 2 And H 2 The problem of O competitive adsorption means that the gas produced by the desorption tower is CO 2 -H 2 O mixed gas, how to efficiently separate H in produced gas 2 O pair to obtain high CO 2 The gas production concentration and the DAC trapping energy consumption under the requirement of reducing the high gas production concentration are important.
Therefore, development of a method for efficiently separating H from gas produced by fully utilizing heat pump cold and heat is needed 2 O thereby obtaining a high gas-generating concentration heat pump driven DAC system.
Disclosure of Invention
In view of the above-mentioned shortcomings in the prior art, the present invention provides a CO 2 The invention discloses a recycling purging heat pump driven direct air carbon capturing system and a method thereof, which deeply digs the matching relation of cold and heat between a heat pump subsystem and a DAC subsystem, and utilizes a heat pump condenser and an evaporator to respectively recycle CO (carbon monoxide) 2 Purge gas and H in produced gas 2 O condensation provides heat and cold energy, realizing high efficiencyThe energy supply mode of the system greatly reduces the comprehensive energy consumption of DAC trapping, separation and purification, and effectively improves the comprehensive energy utilization efficiency of the system.
The invention provides the following technical scheme:
CO (carbon monoxide) 2 The heat pump driven direct air carbon capture system of the recirculation purge comprises a heat pump subsystem and a DAC subsystem (i.e. direct air carbon capture subsystem): the heat pump subsystem and the DAC subsystem are used for coupling heat and cold, wherein a heat pump evaporator of the heat pump subsystem is used for condensing H in produced gas in the DAC subsystem 2 The first condenser of O provides cold energy; part of the high-voltage CO generated by the DAC subsystem 2 And the gas is heated by a heat pump condenser of the heat pump subsystem to provide desorption heat for an adsorption tower of the DAC subsystem.
The heat pump subsystem includes a heat pump evaporator for providing cold to the outside and a heat pump condenser for providing heat.
After gas (such as air) enters the DAC subsystem, adsorption and desorption are carried out to obtain gas (CO) 2 /H 2 O-mixed gas); condensing by a first condenser, wherein H 2 O is condensed and discharged to obtain high-purity CO 2 . Compressed high purity CO 2 A part is collected into CO 2 In the product tank, the other part is heated by the heating pipeline of the heat pump condenser and then returns to the adsorption tower of the heat pump subsystem, so as to provide sufficient desorption energy for the adsorption tower in a desorption state, thereby further improving CO 2 Product concentration.
The invention can adopt various forms of direct air carbon capture subsystem structures as the DAC subsystem; furthermore, the DAC cycle comprising the adsorption tower and the first condenser can be used as the DAC subsystem, and the connection mode and the like can adopt the connection mode disclosed by the invention. Preferably, the DAC subsystem employs a temperature swing vacuum adsorption (TVSA) mode.
As a further preference, the DAC subsystem comprises:
a first adsorption tower and a second adsorption tower which alternately perform adsorption and desorption;
high-temperature CO which is respectively connected with the air inlets of the first adsorption tower and the second adsorption tower and is used for providing desorption heat 2 Inlet pipe, two high temperature CO 2 The inlet pipe is connected with a heating pipeline of the heat pump condenser through a three-way valve;
the two air inlet pipes are connected with the fan through a three-way valve; an input for a gas to be treated;
A treated gas outlet pipe, a vacuum exhaust outlet pipe and a produced gas discharge pipe which are respectively connected with the air outlets of the first adsorption tower and the second adsorption tower, wherein one or more switching valves are arranged on the treated gas outlet pipe, the vacuum exhaust outlet pipe and the produced gas discharge pipe; the other end of the vacuum exhaust outlet pipe is connected with a vacuum pump, and the other end of the gas production discharge pipe is connected with a condensation pipeline of the first condenser.
The treated gas outlet pipe is used for discharging the adsorbed gas; the vacuum exhaust outlet pipe is used for realizing vacuum pumping before desorption; the gas production discharge pipe is used for desorbing CO 2 -H 2 And outputting the O mixed gas.
The treatment gas outlet pipes are respectively provided with a switching valve for controlling the connection and the disconnection of the pipeline; the two treated gas outlet pipes are respectively connected with the air outlets of the first adsorption tower and the second adsorption tower.
The vacuum exhaust outlet pipe is connected with the vacuum pump and is connected with air outlets of the first adsorption tower and the second adsorption tower respectively through branch pipelines with switching valves, and vacuum pumping is carried out on the adsorption towers in a desorption state.
The gas production discharge pipe is also connected with the air outlets of the first adsorption tower and the second adsorption tower respectively through branch pipelines with switching valves; the other end is condensed by a first condenser and then is connected with a compressor, and then is connected with the final CO through a pipeline with a switching valve 2 The storage gas cylinders are connected.
At the same time by arranging a heat pump CO 2 Inflow pipe for introducing a part of high-temperature CO 2 Diverting to a heat pump condenser to be used as a heat source in desorption of the first adsorption tower and the second adsorption towerIs used.
Preferably, the system further comprises a second condenser for primarily condensing the mixed gas, wherein the gas produced after the primary condensation of the second condenser enters the first condenser to be further condensed. The condensing pipeline inlet of the second condenser is connected with the gas outlet of the adsorption tower (the first adsorption tower and the second adsorption tower) of the DAC subsystem through a pipeline with a valve, and the condensing pipeline outlet of the second condenser is connected with the condensing pipeline inlet of the first condenser; the condensing medium pipeline of the second condenser can be connected with a natural cold source to obtain cold energy.
As a further preferred option, a cooling tower is used to provide a cold source for the second condenser. At this time, the cooling tower is connected with a condensing medium pipeline of the second condenser through a cooling pipeline; according to the flow direction, the circulation loop is sequentially provided with: the cooling tower, the cooling water tank, the cooling water pump and the condensing medium pipeline of the second condenser.
An internal cooling source for providing adsorption cooling capacity for the adsorption towers (the first adsorption tower and the second adsorption tower) of the DAC subsystem can be further arranged according to the requirement, and the internal cooling source can be determined by an evaporative cooler or a cooling tower. Preferably, the device further comprises an evaporative cooler or a cooling tower, wherein the evaporative cooler or the cooling tower is connected with the adsorption tower of the DAC subsystem through a pipeline, so as to provide adsorption cooling capacity for the adsorption tower.
Preferably, when an evaporative cooler is adopted, the processing gas and air discharged by the DAC subsystem are mixed according to a set proportion (determined according to the requirement), and then are subjected to heat exchange with an internal cold source in the evaporative cooler and are cooled, and the generated low-temperature internal cold source is used for providing the adsorption cold quantity. According to the medium flow direction, a medium pipeline of the evaporative cooler sequentially forms a circulation loop with an internal cold source water tank, an internal cold source water pump and cooling pipelines of an adsorption tower (a first adsorption tower and a second adsorption tower) through pipelines; the inlets and outlets of the cooling pipelines of the first adsorption tower and the second adsorption tower are respectively connected with the cooling medium inlets of the internal cold source water pump or the evaporative cooler through pipelines with three-way valves.
When the cooling tower is adopted, the cooling tower sequentially forms a circulation loop with an internal cold source water tank, an internal cold source water pump and cooling pipelines of the adsorption towers (a first adsorption tower and a second adsorption tower) according to the flow direction of a cooling medium; the inlets and outlets of the cooling pipelines of the first adsorption tower and the second adsorption tower are respectively connected with the cooling medium inlets of the internal cold source water pump or the evaporative cooler through pipelines with three-way valves.
Preferably, the device also comprises a regenerator for recovering waste heat of the high-temperature produced gas, wherein the outlet of a condensing pipeline of the first condenser is connected with a low-temperature pipeline of the regenerator, and low-temperature high-concentration CO passes through the first condenser 2 Heat exchange with the high-temperature gas produced from the adsorption tower is carried out in a regenerator for recovering the waste heat of the high-temperature gas produced and preheating low-temperature high-concentration CO 2 . Similarly, according to the medium flow direction, the medium pipeline of the first condenser is sequentially connected with the heat pump evaporator, the cold water tank and the cold water pump to form a circulation loop, so that the condensation of materials in the condensation pipeline is realized.
Compared with the traditional heat pump driving DAC system, the invention has the following advantages:
1. the invention is based on the use of CO 2 The TVSA circulating DAC trapping subsystem for recycling and purging carries out deep analysis on heat and cold quantity matching between DAC and heat pump, and the condenser and the evaporator of the heat pump are respectively used for recycling CO 2 Purge gas and H in produced gas 2 The condensation of O provides heat and cold energy, so that an efficient energy supply mode is realized, and the comprehensive energy consumption of capturing, separating and purifying of the DAC subsystem is greatly reduced;
2. the invention realizes the double utilization of the heat side and the cold side of the heat pump, greatly improves the utilization efficiency of the cold and hot of the heat pump subsystem, and effectively reduces the overall energy consumption of the heat pump subsystem;
3. the invention adopts CO 2 The recycling purging mode is used for regenerating the adsorption tower, so that a desorption process with quick dynamics and high gas concentration is realized;
4. According to the invention, natural cold sources generated by evaporative cooling or cooling towers are introduced into the adsorption towers to realize internal cooling adsorption, so that adverse effects of adsorption heat on the adsorption process are reduced, the adsorption rate and the adsorption quantity can be greatly improved, and the trapping efficiency of the DAC subsystem is improved;
5. the invention uses cold water generated by the evaporator of the heat pump subsystem for H in the gas production of the DAC subsystem 2 The condensation and separation process of O provides stable and efficient cold energy supply for condensation, and cooling water generated by a cooling tower can be used for preliminary condensation, so that the condensation energy consumption can be effectively reduced and the gas concentration can be improved;
6. according to the invention, the cold and heat quantity between the heat pump subsystem and the DAC subsystem is efficiently integrated and distributed, the latent heat of the dry air in the adsorption process is recovered through the evaporative cooler and is converted into the cold quantity of the internal cold source, so that the internal cold adsorption is realized, and meanwhile, the waste heat of high-temperature produced gas is recovered through the additionally arranged regenerator, so that the overall operation energy consumption of the whole system is greatly reduced, and the comprehensive energy utilization efficiency of the system is improved;
7. the invention can be operated according to various embodiments in the above manner, and users can flexibly select according to different requirements (such as heat pump performance, gas production concentration, energy consumption requirement, environmental conditions and the like).
Drawings
FIG. 1 is CO in example 1 2 A heat pump driven direct air carbon capture system structure schematic diagram of recirculation purge;
FIG. 2 is CO in example 2 2 A heat pump driven direct air carbon capture system structure schematic diagram of recirculation purge;
FIG. 3 is CO in example 3 2 A heat pump driven direct air carbon capture system structure schematic diagram of recirculation purge;
FIG. 4 is CO in example 4 2 A heat pump driven direct air carbon capture system structure schematic diagram of recirculation purge;
FIG. 5 is CO in example 5 2 The heat pump driven direct air carbon capture system of the recycle purge is structurally schematic.
In the figure:
1. blower 16, eighth switching valve 31, second condenser
2. First air inlet pipe 17, first condenser 32, and cooling water pump
3. First switching valve 18, CO 2 Gas storage bottle 33, cooling water tank
4. Second switching valve 19, ninth switching valve 34, and cooling tower
5. High temperature CO 2 Inlet pipe 20, compressor 35, eleventh switching valve
6. First adsorption tower 21, tenth switching valve 36, twelfth switching valve
7. Second adsorption tower 22, heat pump CO 2 Inflow pipe 37, internal cold source water pump
8. Third switching valve 23, heat pump CO 2 Outflow pipe 38, internal cold source water tank
9. Fourth switching valve 24, heat pump 39 and evaporative cooler
10. Fifth switching valve 25, heat pump condenser 40, and air mixing inlet pipe
11. Sixth switching valve 26, heat pump evaporator 41, thirteenth switching valve
12. Process gas outlet pipe 27, heat pump cold water inflow pipe 42, and second air inlet pipe
13. Seventh switching valve 28, heat pump cold water outflow 43, and exhaust gas discharge pipe
14. Vacuum pump 29, cold water tank 44 and regenerator
15. Vacuum exhaust outlet pipe 30, cold water pump
Detailed Description
The following description of the embodiments is made with reference to the accompanying drawings:
example 1: CO 2 Recycling and blowing for regeneration, and taking heat pump cold water as a condensation cold source
As shown in FIG. 1, the present invention provides a CO 2 The device is a composite system consisting of a heat pump and a DAC, and comprises a fan 1, a first air inlet pipe 2, a first switching valve 3, a second switching valve 4 and a high-temperature CO 2 An inlet pipe 5, a first adsorption tower 6, a second adsorption tower 7, a third switching valve 8, a fourth switching valve 9, a fifth switching valve 10, a sixth switching valve 11, a treated gas outlet pipe 12, a seventh switching valve 13, and a true switching valve An air pump 14, a vacuum exhaust outlet pipe 15, an eighth switching valve 16, a first condenser 17, CO 2 Storage gas cylinder 18, ninth switching valve 19, compressor 20, tenth switching valve 21, heat pump CO 2 Inflow pipe 22, heat pump CO 2 An outflow pipe 23, a heat pump 24, a heat pump condenser 25, a heat pump evaporator 26, a heat pump cold water inflow pipe 27, a heat pump cold water outflow pipe 28, a cold water tank 29 and a cold water pump 30.
The heat pump 24 comprises a heat pump condenser 25 and a heat pump evaporator 26, wherein the heat pump condenser 25 is used for providing heat to the outside, and the heat pump evaporator 26 is used for providing cold to the outside; the first adsorption tower 6, the second adsorption tower 7 and the heat pump 24 pass through CO 2 The purging pipeline is connected; the first condenser 17 is connected to the heat pump 24 via a cold water line.
Wherein, the first switching valve 3 and the second switching valve 4 adopt three-way valves.
The connection mode is as follows:
wherein the fan 1 is connected to a first end of a first switching valve 3 through a first air inlet pipe 2; the second end of the first switching valve 3 is connected with the air inlet of the first adsorption tower 6, and the third end of the first switching valve 3 is connected with the air inlet of the second adsorption tower 7; the air outlet at the other end of the first adsorption tower 6 is connected with a treated air outlet pipe 12 through a fifth switching valve 10; the gas outlet at the other end of the second adsorption tower 7 is connected with a treated gas outlet pipe 12 through a sixth switching valve 11.
One end of the third switching valve 8 is connected to a pipeline between the fifth switching valve 10 and the first adsorption tower 6, and the other end of the third switching valve is connected with one end of the fourth switching valve 9; the other end of the fourth switching valve 9 is connected to a pipeline between the sixth switching valve 11 and the second adsorption tower 7; one end of the seventh switching valve 13 is connected to a pipeline between the third switching valve 8 and the fourth switching valve 9; the other end of the seventh switching valve 13 is connected to a vacuum exhaust outlet pipe 15 through a vacuum pump 14.
One end of the eighth switching valve 16 is connected to a line between the third switching valve 8 and the fourth switching valve 9, and the other end is connected to one end (inlet end) of the condensation line in the first condenser 17; the other end (outlet end) of the condensing pipeline of the first condenser 17 is connected with the inlet of the compressor 20, and the other end of the compressor 20 passes through a ninthSwitching valve 19 and CO 2 The inlet of the storage cylinder 18 is connected.
One end of the tenth switching valve 21 is connected to a pipeline between the compressor 20 and the ninth switching valve 19, and the other end passes through the heat pump CO 2 The inflow pipe 22 is connected to a heat pump condenser 25; heat pump CO 2 The outflow pipe 23 is connected to a heat pump condenser 25 and is fed with high temperature CO 2 The inlet pipe 5 is connected to a first end of the second switching valve 4; the second end of the second switching valve 4 is connected to a pipeline between the first switching valve 3 and the first adsorption tower 6, and the third end is connected to a pipeline between the first switching valve 3 and the second adsorption tower 7.
One end of a cold water tank 29 is connected to the heat pump evaporator 26 through a heat pump cold water outflow pipe 28, and the other end is connected to one end of a cold water pump 30; the other end of the cold water pump 30 is connected with one end of the medium pipeline in the first condenser 17; the other end of the medium line in the first condenser 17 is connected to a heat pump evaporator 26 via a heat pump cold water inlet 27.
The working flow is as follows: taking the case where the second adsorption tower 7 is in an adsorption state and the first adsorption tower 6 is in a desorption state, as an example:
in a specific flow, the second adsorption tower 7 is in an adsorption state, at this time, the end of the first switching valve 3 connected to the first adsorption tower 6 is closed, the fourth switching valve 9 is closed, and the fifth switching valve 10 is closed. Under the drive of the fan 1, the air sequentially enters the second adsorption tower 7 through the air inlet pipe 2 and the first switching valve 3, and CO in the air 2 And H 2 O is absorbed by the solid adsorbent in the second adsorption tower 7, and low CO flows out 2 、H 2 The O process gas is discharged out of the system through the sixth switching valve 11 and the process gas outlet pipe 12 in this order.
In a specific flow, the first adsorption column 6 is in a desorption state, and the third switching valve 8 and the seventh switching valve 13 are opened. Starting a vacuum pump 14, and exhausting residual air in the first adsorption tower 6 through a third switching valve 8 and a seventh switching valve 13 through a vacuum exhaust outlet pipe 15 under the drive of the vacuum pump 14; then the seventh switching valve 13 and the vacuum pump 14 are closed, and the third switching valve 8 and the eighth switching valve 16 are opened; CO desorbed from the first adsorption tower 2 -H 2 O mixingThe gas sequentially passes through a third switching valve 8 and an eighth switching valve 16 and enters a first condenser 17 to produce gas H 2 O is condensed and discharged by a first condenser 17, and the residual high concentration CO 2 The gas is pressurized into the compressor 20; a part of the pressurized gas enters the CO through a ninth switching valve 19 2 In the storage cylinder 18, the other part passes through a tenth switching valve 21 and a heat pump CO 2 The inflow pipe 22 enters the heat pump condenser 25 to be heated; high temperature CO after heating 2 The gas sequentially passes through the heat pump CO 2 Outflow pipe 23, high temperature CO 2 The inlet pipe 5 and the second switching valve 4 enter the first adsorption tower 6 to be purged, and heat is provided for desorption; CO purged out 2 Gas and desorbed CO 2 -H 2 O flows out of the first adsorption tower 6 through the third switching valve 8, and then repeats the above-described flow through the eighth switching valve 16.
Cold water circulates between the heat pump evaporator 26 and the first condenser 17 by being driven by the cold water pump 30; cold water flowing out from the heat pump evaporator 26 sequentially passes through the heat pump cold water outflow pipe 28, the cold water tank 29 and the cold water pump 30 to enter the first condenser 17 to be H in produced gas 2 The condensation of O provides cold energy; the cold water flowing out through the first condenser 17 flows back into the heat pump evaporator 26 through the heat pump cold water inflow pipe 27.
The first adsorption tower 6 is in desorption and the second adsorption tower 7 is in adsorption, and then the operation states are switched respectively, and the first adsorption tower 6 and the second adsorption tower 7 are in circulation and alternately enter the desorption state and the adsorption state, so that the DAC device generally realizes continuous adsorption or continuous gas production.
Advantages are:
the embodiment fully utilizes the heat and cold of the condensing side and the evaporating side of the heat pump to the desorption and condensation process of the DAC, so that the full utilization of the heat and the cold of the heat pump is realized; heating CO by heat pump condensation heat 2 The device is subjected to purging regeneration, so that the desorption rate is accelerated, and the gas production concentration is effectively improved; simultaneously, the cold energy of the heat pump system is fully utilized to carry out CO 2 And H 2 Separation of O, thereby further improving CO 2 Is a trapping concentration of (a).
Example 2: CO 2 The recycle purge is used for regeneration,the cooling water of the cooling tower is used as a primary condensation cold source, and the cold water of the heat pump is used as a deep condensation cold source
As shown in FIG. 2, the present invention provides a CO 2 The heat pump driven direct air carbon capturing system with recirculation purging comprises a fan 1, a first air inlet pipe 2, a first switching valve 3, a second switching valve 4 and a high-temperature CO 2 Inlet pipe 5, first adsorption tower 6, second adsorption tower 7, third switching valve 8, fourth switching valve 9, fifth switching valve 10, sixth switching valve 11, treated gas outlet pipe 12, seventh switching valve 13, vacuum pump 14, vacuum exhaust outlet pipe 15, eighth switching valve 16, first condenser 17, CO 2 Storage gas cylinder 18, ninth switching valve 19, compressor 20, tenth switching valve 21, heat pump CO 2 Inflow pipe 22, heat pump CO 2 An outflow pipe 23, a heat pump 24, a heat pump condenser 25, a heat pump evaporator 26, a heat pump cold water inflow pipe 27, a heat pump cold water outflow pipe 28, a cold water tank 29, a cold water pump 30, a second condenser 31, a cooling water pump 32, a cooling water tank 33, and a cooling tower 34.
The heat pump 24 comprises a heat pump condenser 25 and a heat pump evaporator 26, wherein the heat pump condenser 25 is used for providing heat to the outside, and the heat pump evaporator 26 is used for providing cold to the outside; the first adsorption tower 6, the second adsorption tower 7 and the heat pump 24 pass through CO 2 The purging pipeline is connected; the first condenser 17 is connected with the heat pump 24 through a cold water pipeline; the second condenser 31 is connected to the cooling tower 34 through a cooling water line.
The connection mode is as follows:
wherein the fan 1 is connected to a first end of a first switching valve 3 through a first air inlet pipe 2; the second end of the first switching valve 3 is connected with the air inlet of the first adsorption tower 6, and the third end is connected with the air inlet of the second adsorption tower 7; the air outlet at the other end of the first adsorption tower 6 is connected with a treated air outlet pipe 12 through a fifth switching valve 10; the gas outlet at the other end of the second adsorption tower 7 is connected with a treated gas outlet pipe 12 through a sixth switching valve 11.
One end of the third switching valve 8 is connected to a pipeline between the fifth switching valve 10 and the first adsorption tower 6, and the other end of the third switching valve is connected with one end of the fourth switching valve 9; the other end of the fourth switching valve 9 is connected to a pipeline between the sixth switching valve 11 and the second adsorption tower 7; one end of the seventh switching valve 13 is connected to a pipeline between the third switching valve 8 and the fourth switching valve 9; the other end of the seventh switching valve 13 is connected to a vacuum exhaust outlet pipe 15 through a vacuum pump 14.
One end of the eighth switching valve 16 is connected to a pipeline between the third switching valve 8 and the fourth switching valve 9, and the other end is connected to one end of a condensation pipeline in the second condenser 31; the other end of the condensation pipeline in the second condenser 31 is connected with one end of the condensation pipeline in the first condenser 17; the other end of the condensation pipeline in the first condenser 17 is connected with a compressor 20, and the other end of the compressor 20 is connected with CO through a ninth switching valve 19 2 The storage cylinder 18 is connected.
One end of the tenth switching valve 21 is connected to a pipeline between the compressor 20 and the ninth switching valve 19, and the other end passes through the heat pump CO 2 The inflow pipe 22 is connected to a heat pump condenser 25; heat pump CO 2 The outflow pipe 23 is connected to a heat pump condenser 25 and is fed with high temperature CO 2 The inlet pipe 5 is connected to a first end of the second switching valve 4; the second end of the second switching valve 4 is connected to a pipeline between the first switching valve 3 and the first adsorption tower 6, and the third end is connected to a pipeline between the first switching valve 3 and the second adsorption tower 7.
One end of a cold water tank 29 is connected to the heat pump evaporator 26 through a heat pump cold water outflow pipe 28, and the other end is connected to one end of a cold water pump 30; the other end of the cold water pump 30 is connected with one end of the medium pipeline in the first condenser 17; the other end of the medium line in the first condenser 17 is connected to a heat pump evaporator 26 via a heat pump cold water inlet 27.
One end of the cooling water tank 33 is connected with a cooling water outlet of the cooling tower 34, and the other end is connected with the cooling water pump 32; the other end of the cooling water pump 32 is connected with an inlet of the medium pipeline in the second condenser 31; the other end of the medium line inlet of the second condenser 31 is connected to the cooling water inlet of the cooling tower 34.
The working flow is as follows:
similarly, taking the case where the second adsorption tower 7 is in the adsorption state and the first adsorption tower 6 is in the desorption state, as an example:
the air is driven by the fan 1 to sequentially pass through the air inletThe pipe 2 and the first switching valve 3 enter a second adsorption tower 7, and CO in the air 2 And H 2 O is absorbed by the solid adsorbent in the second adsorption tower 7, and low CO flows out 2 、H 2 The O process gas is discharged out of the system through the sixth switching valve 11 and the process gas outlet pipe 12 in this order.
Starting a vacuum pump 14, and exhausting the air in the first adsorption tower 6 through a vacuum exhaust outlet pipe 15 by sequentially passing through a third switching valve 8 and a seventh switching valve 13 under the drive of the vacuum pump 14; then the seventh switching valve 13 and the vacuum pump 14 are closed, and the eighth switching valve 16 is opened; CO desorbed from the first adsorption tower 2 -H 2 The O mixed gas sequentially enters the second condenser 31 through the third switching valve 8 and the eighth switching valve 16 to be primarily condensed and discharged; CO after preliminary condensation 2 -H 2 The mixed gas of O enters the first condenser 17, H in the mixed gas 2 O is further condensed and discharged, and the residual high concentration CO 2 Into the compressor 20 to be pressurized; a part of the pressurized gas enters the CO through a ninth switching valve 19 2 In the storage cylinder 18, the other part passes through a tenth switching valve 21 and a heat pump CO 2 The inflow pipe 22 enters the heat pump condenser 25 to be heated; high temperature CO after heating 2 The gas sequentially passes through the heat pump CO 2 Outflow pipe 23, high temperature CO 2 The inlet pipe 5 and the second switching valve 4 enter the first adsorption tower 6 to be purged, and heat is provided for desorption; CO purged out 2 Gas and desorbed CO 2 And H 2 O flows out of the first adsorption tower 6 through the third switching valve 8, and then repeats the above-described flow through the eighth switching valve 16.
Cold water circulates between the heat pump evaporator 26 and the first condenser 17 by being driven by the cold water pump 30; cold water flowing out from the heat pump evaporator 26 sequentially passes through the heat pump cold water outflow pipe 28, the cold water tank 29 and the cold water pump 30 to enter the first condenser 17 to be H in produced gas 2 The condensation of O provides cold energy; the cold water flowing out through the first condenser 17 flows back into the heat pump evaporator 26 through the heat pump cold water inflow pipe 27.
The cooling water circulates between the cooling tower 34 and the second condenser 31 by the cooling water pump 32; cooling water flowing out through the cooling tower 34 (fromNatural cold source) sequentially passes through a cooling water tank 33 and a cooling water pump 32 to enter a second condenser 31 to be H in the produced gas 2 The preliminary condensation of O provides cold energy; the cooling water flowing out through the second condenser 31 flows back into the cooling tower 34.
The first adsorption tower 6 is in desorption and the second adsorption tower 7 is in adsorption, and then the operation states are switched respectively, and the first adsorption tower 6 and the second adsorption tower 7 are in circulation and alternately enter the desorption state and the adsorption state, so that the DAC device generally realizes continuous adsorption or continuous gas production.
Advantages are:
this embodiment heats the heat on the condensing side of the heat pump to CO 2 The heat pump is subjected to purging regeneration, and CO is performed by utilizing the cold energy of the evaporation side of the heat pump 2 And H 2 O is separated, so that the gas production concentration is effectively improved; simultaneously, natural cold source of cooling tower is adopted for CO 2 -H 2 H in O mixed gas 2 O preliminary condensation can effectively reduce condensation energy consumption and further improve CO 2 Is a trapping concentration of (a).
Example 3: CO 2 Recycling and blowing to regenerate, using cooling water of cooling tower as primary condensation cold source, using heat pump cold water as deep condensation cold source, using evaporative cooling as internal cold source to promote adsorption
As shown in FIG. 3, the present invention provides a CO 2 The heat pump driven direct air carbon capture system with recirculation purge comprises a fan 1, a first air inlet pipe 2, a first switching valve 3, a second switching valve 4 and a high temperature CO 2 Inlet pipe 5, first adsorption tower 6, second adsorption tower 7, third switching valve 8, fourth switching valve 9, fifth switching valve 10, sixth switching valve 11, treated gas outlet pipe 12, seventh switching valve 13, vacuum pump 14, vacuum exhaust outlet pipe 15, eighth switching valve 16, first condenser 17, CO 2 Storage gas cylinder 18, ninth switching valve 19, compressor 20, tenth switching valve 21, heat pump CO 2 Inflow pipe 22, heat pump CO 2 An outflow pipe 23, a heat pump 24, a heat pump condenser 25, a heat pump evaporator 26, a heat pump cold water inflow pipe 27, a heat pump cold water outflow pipe, a cold water tank 29, a cold water pump 30, a second condenser, a cooling water pump 32, a cooling water tank 33, a cooling tower 34, and an eleventh switchA change valve 35, a twelfth switching valve 36, an internal cold source water pump 37, an internal cold source water tank 38, an evaporative cooler 39, a mixed air inlet pipe 40, a thirteenth switching valve 41, a second air inlet pipe 42, and an exhaust gas discharge pipe 43.
Wherein the heat pump 24 comprises a heat pump condenser 25 and a heat pump evaporator 26; the first adsorption tower 6 and the second adsorption tower 7 pass through CO 2 The purge pipeline is connected with the heat pump 24 and is connected with the evaporative cooler 39 through an internal cold source pipeline; the first condenser 17 is connected with the heat pump 24 through a cold water pipeline; the second condenser 31 is connected to the cooling tower 34 through a cooling water line.
The connection mode is as follows:
wherein the fan 1 is connected to a first end of a first switching valve 3 through a first air inlet pipe 2; the second end of the first switching valve 3 is connected with the air inlet of the first adsorption tower 6, and the third end is connected with the air inlet of the second adsorption tower 7; the air outlet at the other end of the first adsorption tower 6 is connected with a treated air outlet pipe 12 through a fifth switching valve 10; the air outlet at the other end of the second adsorption tower 7 is connected with a treated air outlet pipe 12 through a sixth switching valve 11; the treated gas outlet pipe 12 is connected to the evaporative cooler 39 through a mixed air inlet pipe 40; the second air inlet pipe 42 is connected to the piping between the process air outlet pipe 12 and the air mixing inlet pipe 40 through a thirteenth switching valve 41; the exhaust gas discharge pipe 43 is connected to the evaporative cooler 39.
One end of the third switching valve 8 is connected to a pipeline between the fifth switching valve 10 and the first adsorption tower 6, and the other end of the third switching valve is connected with one end of the fourth switching valve 9; the other end of the fourth switching valve 9 is connected to a pipeline between the sixth switching valve 11 and the second adsorption tower 7; one end of the seventh switching valve 13 is connected to a pipeline between the third switching valve 8 and the fourth switching valve 9; the other end of the seventh switching valve 13 is connected to a vacuum exhaust outlet pipe 15 through a vacuum pump 14.
One end of the eighth switching valve 16 is connected to a pipeline between the third switching valve 8 and the fourth switching valve 9, and the other end is connected to one end of a condensation pipeline in the second condenser 31; the other end of the condensing pipeline of the second condenser 31 is connected with one end of the condensing pipeline of the first condenser 17; the other end of the condensation pipeline of the first condenser 17 is connected with the compressor 20The other end of the compressor 20 is connected to CO through a ninth switching valve 19 2 The storage cylinder 18 is connected.
One end of the tenth switching valve 21 is connected to a pipeline between the compressor 20 and the ninth switching valve 19, and the other end passes through the heat pump CO 2 The inflow pipe 22 is connected to a heat pump condenser 25; heat pump CO 2 The outflow pipe 23 is connected to a heat pump condenser 25 and is fed with high temperature CO 2 The inlet pipe 5 is connected to a first end of the second switching valve 4; the other second end of the second switching valve 4 is connected to a pipeline between the first switching valve 3 and the first adsorption tower 6, and the third end is connected to a pipeline between the first switching valve 3 and the second adsorption tower 7.
One end of a cold water tank 29 is connected to the heat pump evaporator 26 through a heat pump cold water outflow pipe 28, and the other end is connected to one end of a cold water pump 30; the other end of the cold water pump 30 is connected with one end of the medium pipeline in the first condenser 17; the other end of the medium line in the first condenser 17 is connected to a heat pump evaporator 26 via a heat pump cold water inlet 27.
One end of the cooling water tank 33 is connected with the cooling tower 34, and the other end is connected with the cooling water pump 32; the other end of the cooling water pump 32 is connected with the second condenser 31; the other end of the second condenser 31 is connected to a cooling tower 34.
One end of the eleventh switching valve 35 is connected to the first adsorption tower 6, the other end is connected to the second adsorption tower 7, and the third end is connected to the evaporative cooler 39; one end of a twelfth switching valve 36 is connected with the first adsorption tower 6, the other end is connected with the second adsorption tower 7, and the third end is connected with an internal cold source water pump 37; the other end of the internal cold source water pump 37 is connected with an internal cold source water tank 38; the other end of the internal cooling source water tank 38 is connected to an evaporative cooler 39.
The working flow is as follows:
similarly, taking the case where the second adsorption tower 7 is in the adsorption state and the first adsorption tower 6 is in the desorption state, as an example:
under the drive of the fan 1, the air sequentially enters the second adsorption tower 7 through the air inlet pipe 2 and the first switching valve 3, and CO in the air 2 And H 2 O is absorbed by the solid adsorbent in the second adsorption tower 7, and low CO flows out 2 、H 2 O treatment gas valveThe mixed air passes through the sixth switching valve 11 to the treated air outlet pipe 12, is mixed with the air passing through the second air inlet pipe 42 and the thirteenth switching valve 41 according to a certain proportion, enters the evaporative cooler 39 through the mixed air inlet pipe 40, takes away the heat of the internal cooling source to cool the same, and is discharged out of the system through the exhaust gas discharge pipe 43.
Starting a vacuum pump 14, and exhausting the air in the first adsorption tower 6 through a vacuum exhaust outlet pipe 15 by sequentially passing through a third switching valve 8 and a seventh switching valve 13 under the drive of the vacuum pump 14; then the seventh switching valve 13 and the vacuum pump 14 are closed, and the eighth switching valve 16 is opened; CO desorbed from the first adsorption tower 2 -H 2 The O mixed gas sequentially passes through a third switching valve 8 and an eighth switching valve 16 and enters a second condenser 31 to be primarily condensed; the gas produced after preliminary condensation enters a first condenser 17, H in the mixed gas 2 O is further condensed, and the residual high concentration CO 2 The gas is pressurized into the compressor 20; a part of the pressurized gas enters the CO through a ninth switching valve 19 2 In the storage cylinder 18, the other part passes through a tenth switching valve 21 and a heat pump CO 2 The inflow pipe 22 enters the heat pump condenser 25 to be heated; high temperature CO after heating 2 The gas sequentially passes through the heat pump CO 2 Outflow pipe 23, high temperature CO 2 The inlet pipe 5 and the second switching valve 4 enter the first adsorption tower 6 to be purged, and heat is provided for desorption; CO purged out 2 Gas and desorbed CO 2 -H 2 O flows out of the first adsorption tower 6 through the third switching valve 8, and then repeats the above-described flow through the eighth switching valve 16.
Cold water circulates between the heat pump evaporator 26 and the first condenser 17 by being driven by the cold water pump 30; cold water flowing out from the heat pump evaporator 26 sequentially passes through a heat pump cold water outflow pipe 28, a cold water tank 29 and a cold water pump 30 to enter the first condenser 17 to be CO 2 -H 2 H in O mixed gas 2 The condensation of O provides cold energy; the cold water flowing out through the first condenser 17 flows back into the heat pump evaporator 26 through the heat pump cold water inflow pipe 27.
The cooling water circulates between the cooling tower 34 and the second condenser 31 by the cooling water pump 32; flows out through the cooling tower 34The cooling water of (2) sequentially passes through a cooling water tank 33 and a cooling water pump 32 to enter a second condenser 31 to be H in the produced gas 2 The preliminary condensation of O provides cold energy; the cooling water flowing out through the second condenser 31 flows back into the cooling tower 34.
The internal cold source flowing out through the evaporative cooler 39 sequentially passes through the internal cold source water tank 38, the internal cold source water pump 37 and the twelfth switching valve 36 to enter the second adsorption tower 7, so that adsorption heat generated in the adsorption process is taken away, and the adsorption process is effectively promoted; the internal cooling source flowing out through the second adsorption tower 7 flows back to the evaporative cooler 39 through the eleventh switching valve 35.
The first adsorption tower 6 is in desorption and the second adsorption tower 7 is in adsorption, and then the operation states are switched respectively, and the first adsorption tower 6 and the second adsorption tower 7 are in circulation and alternately enter the desorption state and the adsorption state, so that the DAC device generally realizes continuous adsorption or continuous gas production.
Advantages are:
this embodiment heats the heat pump condensation side heat to CO 2 The heat pump is subjected to purging regeneration, and CO is performed by utilizing the cold energy of the evaporation side of the heat pump 2 And H 2 O is separated, so that the gas production concentration is effectively improved; meanwhile, natural cold source of cooling tower is adopted to produce H in gas 2 O preliminary condensation can effectively reduce condensation energy consumption and further improve CO 2 Is a trapping concentration of (1); in addition, the low H of the treatment is fully utilized 2 The characteristic of O content ensures that the adsorption tower generates an internal cold source for internal cooling of the adsorption tower through the evaporative cooler, greatly promotes the adsorption process and can effectively improve CO 2 The capture amount realizes the increase of energy utilization conversion efficiency in the DAC cycle process.
Example 4: CO 2 Recycling and blowing to regenerate, taking heat pump cold water as a condensation cold source, and taking cooling tower cooling water as an internal cold source to promote adsorption
As shown in FIG. 4, the present invention provides a CO 2 The heat pump driven direct air carbon capturing system with recirculation purging comprises a fan 1, a first air inlet pipe 2, a first switching valve 3, a second switching valve 4 and a high-temperature CO 2 Inlet pipe 5, first adsorption tower 6, second adsorption tower 7, third switchValve 8, fourth switching valve 9, fifth switching valve 10, sixth switching valve 11, process gas outlet pipe 12, seventh switching valve 13, vacuum pump 14, vacuum exhaust outlet pipe 15, eighth switching valve 16, first condenser 17, CO 2 Storage gas cylinder 18, ninth switching valve 19, compressor 20, tenth switching valve 21, heat pump CO 2 Inflow pipe 22, heat pump CO 2 An outflow pipe 23, a heat pump 24, a heat pump condenser 25, a heat pump evaporator 26, a heat pump cold water inflow pipe 27, a heat pump cold water outflow pipe 28, a cold water tank 29, a cold water pump 30, a cooling tower 34, an eleventh switching valve 35, a twelfth switching valve 36, an internal cold source water pump 37, and an internal cold source water tank 38. Wherein the heat pump 24 comprises a heat pump condenser 25 and a heat pump evaporator 26; the first adsorption tower 6, the second adsorption tower 7 and the heat pump 24 pass through CO 2 The purging pipeline is connected with the cooling tower 34 through an internal cold source pipeline; the first condenser 17 is connected to the heat pump 24 via a cold water line.
The connection mode is as follows:
wherein the fan 1 is connected to a first end of a first switching valve 3 through a first air inlet pipe 2; the second end of the first switching valve 3 is connected with the air inlet of the first adsorption tower 6, and the third end is connected with the air inlet of the second adsorption tower 7; the air outlet at the other end of the first adsorption tower 6 is connected with a treated air outlet pipe 12 through a fifth switching valve 10; the gas outlet at the other end of the second adsorption tower 7 is connected with a treated gas outlet pipe 12 through a sixth switching valve 11.
One end of the third switching valve 8 is connected to a pipeline between the fifth switching valve 10 and the first adsorption tower 6, and the other end of the third switching valve is connected with one end of the fourth switching valve 9; the other end of the fourth switching valve 9 is connected to a pipeline between the sixth switching valve 11 and the second adsorption tower 7; one end of the seventh switching valve 13 is connected to a pipeline between the third switching valve 8 and the fourth switching valve 9; the other end of the seventh switching valve 13 is connected to a vacuum exhaust outlet pipe 15 through a vacuum pump 14.
One end of the eighth switching valve 16 is connected to a pipeline between the third switching valve 8 and the fourth switching valve 9, and the other end is connected to one end of the first condenser 17; the other end of the first condenser 17 is connected with a compressor 20, and the other end of the compressor 20 is connected with CO through a ninth switching valve 19 2 Storage gasThe bottles 18 are connected.
One end of the tenth switching valve 21 is connected to a pipeline between the compressor 20 and the ninth switching valve 19, and the other end passes through the heat pump CO 2 The inflow pipe 22 is connected to a heat pump condenser 25; heat pump CO 2 The outflow pipe 23 is connected to a heat pump condenser 25 and is fed with high temperature CO 2 The inlet pipe 5 is connected to a first end of the second switching valve 4; the second end of the second switching valve 4 is connected to a pipeline between the first switching valve 3 and the first adsorption tower 6, and the third end is connected to a pipeline between the first switching valve 3 and the second adsorption tower 7.
One end of the cold water tank 29 is connected to the heat pump evaporator 26 through a heat pump cold water outflow pipe 28, the other end is connected with one end of the cold water pump 30; the other end of the cold water pump 30 is connected with one end of the medium pipeline in the first condenser 17; the other end of the medium line in the first condenser 17 is connected to a heat pump evaporator 26 via a heat pump cold water inlet 27.
One end of the eleventh switching valve 35 is connected to the first adsorption tower 6, the other end is connected to the second adsorption tower 7, and the third end is connected to the cooling tower 34; one end of a twelfth switching valve 36 is connected with the first adsorption tower 6, the other end is connected with the second adsorption tower 7, and the third end is connected with an internal cold source water pump 37; the other end of the internal cold source water pump 37 is connected with an internal cold source water tank 38; the other end of the internal cooling source water tank 38 is connected to the cooling tower 34.
The working flow is as follows:
similarly, taking the case where the second adsorption tower 7 is in the adsorption state and the first adsorption tower 6 is in the desorption state, as an example:
under the drive of the fan 1, the air sequentially enters the second adsorption tower 7 through the air inlet pipe 2 and the first switching valve 3, and CO in the air 2 And H 2 O is absorbed by the solid adsorbent in the second adsorption tower 7, and low CO flows out 2 、H 2 The O process gas is discharged out of the system through the sixth switching valve 11 and the process gas outlet pipe 12 in this order.
Starting a vacuum pump 14, and exhausting the air in the first adsorption tower 6 through a vacuum exhaust outlet pipe 15 by sequentially passing through a third switching valve 8 and a seventh switching valve 13 under the drive of the vacuum pump 14; then the seventh switching valve 13 and the vacuum pump 14 are closed, from the first suctionCO desorbed by tower 2 -H 2 The mixed gas of O sequentially passes through the third switching valve 8 and the eighth switching valve 16 to enter the first condenser 17, and H in the mixed gas 2 O is condensed and discharged by a first condenser 17, and the residual high concentration CO 2 The gas is pressurized into the compressor 20; a part of the pressurized gas enters the CO through a ninth switching valve 19 2 In the storage cylinder 18, the other part passes through a tenth switching valve 21 and a heat pump CO 2 The inflow pipe 22 enters the heat pump condenser 25 to be heated; high temperature CO after heating 2 The gas sequentially passes through the heat pump CO 2 Outflow pipe 23, high temperature CO 2 The inlet pipe 5 and the second switching valve 4 enter the first adsorption tower 6 to be purged, and heat is provided for desorption; CO purged out 2 Gas and desorbed CO 2 -H 2 O flows out of the first adsorption tower 6 through the third switching valve 8, and then repeats the above-described flow through the eighth switching valve 16.
Cold water circulates between the heat pump evaporator 26 and the first condenser 17 by being driven by the cold water pump 30; cold water flowing out from the heat pump evaporator 26 sequentially passes through the heat pump cold water outflow pipe 28, the cold water tank 29 and the cold water pump 30 to enter the first condenser 17 to be H in produced gas 2 The condensation of O provides cold energy; the cold water flowing out through the first condenser 17 flows back into the heat pump evaporator 26 through the heat pump cold water inflow pipe 27.
The internal cold source flowing out from the cooling tower 34 sequentially passes through an internal cold source water tank 38, an internal cold source water pump 37 and a twelfth switching valve 36 to enter the second adsorption tower 7, so that adsorption heat generated in the adsorption process is taken away, and the adsorption process is promoted; the internal cooling source flowing out through the second adsorption tower 7 is returned to the cooler tower 34 through the eleventh switching valve 35.
The first adsorption tower 6 is used for completing desorption, and the second adsorption tower 7 is used for completing adsorption, and then the operation states are respectively switched, so that the DAC device generally realizes the continuous adsorption or continuous gas production function.
Advantages are:
this embodiment utilizes heat pump condensation heat to heat CO 2 The air is subjected to purging regeneration, and the evaporation side cooling capacity is utilized to H in the produced gas 2 O condensation process can effectively improve CO 2 Is trapped in (a)Concentration; in addition, the natural cold source with low cost is adopted to cool the adsorption process of the adsorption tower, so that the CO can be improved 2 The adsorption and trapping amount of the DAC device are improved, and the overall operation benefit of the DAC device is improved.
Example 5: CO 2 Recycling and blowing for regeneration, and taking heat pump cold water as a condensation cold source with heat recovery
As shown in FIG. 5, the present invention provides a CO 2 The system is a composite system obtained by coupling a heat pump and a DAC, and comprises a fan 1, a first air inlet pipe 2, a first switching valve 3, a second switching valve 4 and a high-temperature CO 2 Inlet pipe 5, first adsorption tower 6, second adsorption tower 7, third switching valve 8, fourth switching valve 9, fifth switching valve 10, sixth switching valve 11, treated gas outlet pipe 12, seventh switching valve 13, vacuum pump 14, vacuum exhaust outlet pipe 15, eighth switching valve 16, first condenser 17, CO 2 Storage gas cylinder 18, ninth switching valve 19, compressor 20, tenth switching valve 21, heat pump CO 2 Inflow pipe 22, heat pump CO 2 An outflow pipe 23, a heat pump 24, a heat pump condenser 25, a heat pump evaporator 26, a heat pump cold water inflow pipe 27, a heat pump cold water outflow pipe 28, a cold water tank 29, a cold water pump 30 and a regenerator 44. Wherein the heat pump 24 comprises a heat pump condenser 25 and a heat pump evaporator 26; the first adsorption tower 6, the second adsorption tower 7 and the heat pump 24 pass through CO 2 The purging pipeline is connected; the first condenser 17 is connected to the heat pump 24 via a cold water line.
The connection mode is as follows:
wherein the fan 1 is connected to a first end of a first switching valve 3 through a first air inlet pipe 2; the second end of the first switching valve 3 is connected with the air inlet of the first adsorption tower 6, and the third end is connected with the air inlet of the second adsorption tower 7; the air outlet at the other end of the first adsorption tower 6 is connected with a treated air outlet pipe 12 through a fifth switching valve 10; the gas outlet at the other end of the second adsorption tower 7 is connected with a treated gas outlet pipe 12 through a sixth switching valve 11.
One end of the third switching valve 8 is connected to a pipeline between the fifth switching valve 10 and the first adsorption tower 6, and the other end of the third switching valve is connected with one end of the fourth switching valve 9; the other end of the fourth switching valve 9 is connected to a pipeline between the sixth switching valve 11 and the second adsorption tower 7; one end of the seventh switching valve 13 is connected to a pipeline between the third switching valve 8 and the fourth switching valve 9; the other end of the seventh switching valve 13 is connected to a vacuum exhaust outlet pipe 15 through a vacuum pump 14.
One end of the eighth switching valve 16 is connected to a pipeline between the third switching valve 8 and the fourth switching valve 9, and the other end is connected to one end (inlet end) of a high-temperature pipeline in the regenerator 44; the other end (outlet end) of the high-temperature pipeline in the heat regenerator 44 is connected with one end (inlet end) of the condensation pipeline in the first condenser 17, the inlet end of the low-temperature pipeline of the heat regenerator 44 is connected with the outlet end of the condensation pipeline in the first condenser 17, and the outlet end of the low-temperature pipeline of the heat regenerator 44 is connected with the compressor 20; the other end of the compressor 20 is connected with CO through a ninth switching valve 19 2 The storage cylinder 18 is connected.
One end of the tenth switching valve 21 is connected to a pipeline between the compressor 20 and the ninth switching valve 19, and the other end passes through the heat pump CO 2 The inflow pipe 22 is connected to a heat pump condenser 25; heat pump CO 2 The outflow pipe 23 is connected to a heat pump condenser 25 and is fed with high temperature CO 2 The inlet pipe 5 is connected to a first end of the second switching valve 4; the second end of the second switching valve 4 is connected to a pipeline between the first switching valve 3 and the first adsorption tower 6, and the third end is connected to a pipeline between the first switching valve 3 and the second adsorption tower 7.
One end of a cold water tank 29 is connected to the heat pump evaporator 26 through a heat pump cold water outflow pipe 28, and the other end is connected to one end of a cold water pump 30; the other end of the cold water pump 30 is connected with one end of the first condenser 17; the other end of the first condenser 17 is connected to a heat pump evaporator 26 through a heat pump cold water inflow port 27.
The working flow is as follows:
taking the case where the second adsorption tower 7 is in an adsorption state and the first adsorption tower 6 is in a desorption state, as an example:
under the drive of the fan 1, the air sequentially enters the second adsorption tower 7 through the air inlet pipe 2 and the first switching valve 3, and CO in the air 2 And H 2 O is absorbed by the solid adsorbent in the second adsorption tower 7, and low CO flows out 2 、H 2 The O process gas is discharged out of the system through the sixth switching valve 11 and the process gas outlet pipe 12 in this order.
Starting a vacuum pump 14, and exhausting the air in the first adsorption tower 6 through a vacuum exhaust outlet pipe 15 by sequentially passing through a third switching valve 8 and a seventh switching valve 13 under the drive of the vacuum pump 14; then the seventh switching valve 13 and the vacuum pump 14 are closed, and the third switching valve 8 and the eighth switching valve 16 are opened; the high-temperature gas flowing out of the first adsorption tower passes through the third switching valve 8, the eighth switching valve 16, the heat regenerator 44 and the first condenser 17 in sequence and then returns to the heat regenerator 44 again, and the high-temperature CO in the heat regenerator 44 2 -H 2 The O-mixed gas heats the low-temperature high-concentration CO flowing out of the first condenser 17 2 On the one hand, the gas can pre-cool high-temperature CO 2 -H 2 O mixed gas, reduces the condensation energy consumption of the first condenser 17, and can preheat low-temperature high-concentration CO 2 Gas, reducing heating energy consumption of the heat pump condenser 25; high concentration CO after preheating 2 The gas is pressurized into the compressor 20; a part of the pressurized gas enters the CO through a ninth switching valve 19 2 In the storage cylinder 18, the other part passes through a tenth switching valve 21 and a heat pump CO 2 The inflow pipe 22 enters the heat pump condenser 25 to be heated; high temperature CO after heating 2 The gas sequentially passes through the heat pump CO 2 Outflow pipe 23, high temperature CO 2 The inlet pipe 5 and the second switching valve 4 enter the first adsorption tower 6 to be purged, and heat is provided for desorption; CO purged out 2 Gas and desorbed CO 2 And H 2 O flows out of the first adsorption tower 6 through the third switching valve 8, and then repeats the above-described flow through the eighth switching valve 16.
Cold water circulates between the heat pump evaporator 26 and the first condenser 17 by being driven by the cold water pump 30; cold water flowing out from the heat pump evaporator 26 sequentially passes through a heat pump cold water outflow pipe 28, a cold water tank 29 and a cold water pump 30 to enter the first condenser 17 to be CO 2 -H 2 H in O mixed gas 2 The condensation of O provides cold energy; the cold water flowing out through the first condenser 17 flows back into the heat pump evaporator 26 through the heat pump cold water inflow pipe 27.
The first adsorption tower 6 is in desorption and the second adsorption tower 7 is in adsorption, and then the operation states are switched respectively, and the first adsorption tower 6 and the second adsorption tower 7 are in circulation and alternately enter the desorption state and the adsorption state, so that the DAC device generally realizes continuous adsorption or continuous gas production.
Advantages are:
this embodiment utilizes heat pump condensation heat to heat CO 2 The air is subjected to purging regeneration, and the evaporation side cooling capacity is utilized to H in the produced gas 2 O condensation process can effectively improve CO 2 Is a trapping concentration of (1); in addition, a regenerator is additionally arranged, and the waste heat of the high-temperature gas production is utilized to heat the low-temperature high-concentration CO flowing out of the first condenser 17 2 The gas can effectively reduce the condensation energy consumption of the first condenser 17 and the heating energy consumption of the heat pump condenser 25, thereby improving the overall energy utilization rate of the DAC device operation and reducing the energy consumption of DAC capturing, separating and purifying.
Claims (9)
1. CO (carbon monoxide) 2 The heat pump driven direct air carbon capture system of recirculation purge, including heat pump subsystem and direct air carbon capture subsystem, its characterized in that: the heat pump subsystem and the direct air carbon capture subsystem are used for coupling heat and cold energy, wherein a heat pump evaporator of the heat pump subsystem is used for condensing H in produced gas in the direct air carbon capture subsystem 2 The first condenser of O provides cold energy; partial high pressure CO generated by the direct air carbon capture subsystem 2 And the gas is heated by a heat pump condenser of the heat pump subsystem to provide desorption heat for an adsorption tower of the direct air carbon capture subsystem.
2. The CO according to claim 1 2 The heat pump driven direct air carbon capture system of recirculation purge, its characterized in that: the direct air carbon capture subsystem adopts a temperature-variable vacuum adsorption type operation mode.
3. The CO according to claim 1 2 The heat pump driven direct air carbon capture system of recirculation purge, its characterized in that: the device also comprises a second condenser for initially condensing the produced gas, and the produced gas passes through the second condenserAnd the gas produced after the condensation step enters the first condenser again to be condensed further.
4. A CO according to claim 3 2 The heat pump driven direct air carbon capture system of recirculation purge, its characterized in that: and providing a natural cold source for the second condenser by using a cooling tower.
5. The CO according to claim 1 2 The heat pump driven direct air carbon capture system of recirculation purge, its characterized in that: the device also comprises an evaporative cooler or a cooling tower, wherein the evaporative cooler or the cooling tower is connected with an adsorption tower of the direct air carbon capture subsystem through a pipeline, and an internal cooling source for adsorption is provided for the adsorption tower.
6. The CO of claim 5 2 The heat pump driven direct air carbon capture system of recirculation purge, its characterized in that: when the evaporative cooler is adopted, the treatment gas discharged by the direct air carbon capture subsystem is mixed with air according to a set proportion, heat of an internal cold source in the evaporative cooler is taken away, and the generated low-temperature internal cold source is used for internal cooling adsorption.
7. The CO according to claim 1 2 The heat pump driven direct air carbon capture system of recirculation purge, its characterized in that: the device also comprises a heat regenerator for recovering waste heat of the produced gas, wherein an outlet of a condensation pipeline of the first condenser is connected with a low-temperature pipeline of the heat regenerator, and low-temperature high-concentration CO condensed by the first condenser 2 Heat exchange with the high-temperature gas produced from the adsorption tower is carried out in a regenerator for recovering the waste heat of the high-temperature gas produced and preheating low-temperature high-concentration CO 2 。
8. A CO according to any one of claims 1 to 7 2 The heat pump driven direct air carbon capture system of recirculation purge, its characterized in that: the direct air carbon capture subsystem mainly comprises:
a first adsorption tower and a second adsorption tower which alternately perform adsorption and desorption;
high-temperature CO which is respectively connected with the air inlets of the first adsorption tower and the second adsorption tower and is used for providing desorption heat 2 The two adsorption towers are connected with a heating pipeline of the heat pump condenser through a three-way valve;
the two air inlet pipes are connected with the fan through a three-way valve;
a treated gas outlet pipe, a vacuum exhaust outlet pipe and a produced gas discharge pipe which are respectively connected with the air outlets of the first adsorption tower and the second adsorption tower, wherein one or more switching valves are arranged on the treated gas outlet pipe, the vacuum exhaust outlet pipe and the produced gas discharge pipe; the vacuum exhaust outlet pipe is connected with the vacuum pump, and the other end of the gas production discharge pipe is connected with the condensation pipeline of the first condenser.
9.CO 2 A heat pump driven direct air carbon capture process with recirculation purge characterized in that CO according to any one of claims 1 to 8 is used 2 The heat pump with recirculation purging drives the direct air carbon trapping system to carry out high-efficiency direct air carbon trapping.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202310897457.6A CN116951803A (en) | 2023-07-20 | 2023-07-20 | CO 2 Heat pump driven direct air carbon capture system with recirculation purging and method thereof |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202310897457.6A CN116951803A (en) | 2023-07-20 | 2023-07-20 | CO 2 Heat pump driven direct air carbon capture system with recirculation purging and method thereof |
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| CN (1) | CN116951803A (en) |
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