CN117190539A - Heat pump driven air direct carbon trapping device based on TVSA circulation - Google Patents
Heat pump driven air direct carbon trapping device based on TVSA circulation Download PDFInfo
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Abstract
The invention discloses a heat pump driven air direct carbon trapping device based on TVSA circulation, which comprises an evaporative cooler, a heat pump subsystem and a DAC subsystem mainly composed of at least two adsorption beds and a first condenser; the heat pump condenser of the heat pump subsystem is connected with the heat exchange channels of the adsorption beds through an internal heat source circulation loop, so that the DAC subsystem is provided with heat desorption; an air inlet of the evaporative cooler is connected with a processing air pipeline of the DAC subsystem through a pipeline, and the latent heat waste heat of the processing air of the DAC subsystem is recovered; medium pipe passing through condensing circulation loop and first condenser simultaneouslyThe paths are connected, and the gas produced by the DAC subsystem is condensed. The invention adopts a TVSA circulating DAC trapping subsystem, utilizes the evaporative cooling of the vapor in the evaporative cooler to convert the low moisture content potential energy in the drying treatment gas of the adsorption outlet into the cold energy of cooling water for desorbing H in the air 2 O condensation and separation, thereby realizing high concentration CO 2 Is a result of the production of (a).
Description
Technical Field
The invention relates to a direct air carbon capture device and a heat pump device, in particular to a heat pump driven air direct carbon capture system based on TVSA.
Background
The global temperature is continuously rising and the climate is becoming increasingly warm. The main reason for climate warming is that human society emits a large amount of greenhouse gases into the atmosphere. And CO 2 As the most widely used greenhouse gas, the current emissions have reached 340 million tons per year. To mitigate global warming, achieving carbon neutralization requires a great deal of development of carbon negative emission technology.
DAC technology is a method for capturing CO directly from the atmosphere by utilizing physical and chemical actions 2 Due to the flexible arrangement, small occupied area of land and water resources, and capability of realizing the clean removal of CO from the atmosphere 2 Therefore, it has become a hot point of research in carbon capture technology in recent years.
The main research direction of the current DAC technology is how to prepare high-performance CO 2 Adsorbents, however, are not very sufficient in terms of system integration and optimization design for DAC trapping devices. In the DAC trapping process, air passes through an absorber under the driving of a fan, and CO in the air 2 Is adsorbed by the adsorbent. Not only CO is adsorbed by the amine functional adsorbent 2 And also absorb a large amount of H at the same time 2 O. Thus, the outlet of the adsorber is low in CO 2 Dry process gas exhaust. CO from TVSA cycle during desorption 2 Desorption is carried out by a cyclic mode of variable temperature vacuum (Temperature Vaccum Swing Adsorption, TVSA). To obtain high concentration of CO 2 The desorbed desorption gas needs to pass through a condenser to make most of H 2 O is condensed off, and the rest is CO with high concentration 2 Product gas.
The primary energy change during DAC cycling is the temperature change process. In the adsorption process, since adsorption is an exothermic process, the temperature of the adsorbent is continuously increased as the adsorption process proceeds. The increase of the adsorption temperature can seriously reduce the equilibrium adsorption quantity of the adsorbent and affect the trapping performance of the DAC device, so that the adsorbent needs to be cooled in the adsorption process. The cooling mode can be divided into two modes of internal cooling of the adsorbent and precooling of the treated air. In addition, in the desorption switching process, the adsorbent and the adsorber are in a higher desorption temperature state, and the temperature of the adsorbent and the adsorber also needs to be reduced by a cooling mode. In the desorption process, the desorption gas needs to be condensed to obtain the high-concentration product gas, and the cold energy required by condensation is also one of the energy input indispensable in the DAC device.
A big problem limiting the large-scale arrangement of DAC devices is the high capture energy consumption. For the heat input required during operation of the DAC device, the capture energy consumption can be reduced by employing efficient thermodynamic equipment. A heat pump is a common heating device with a high COP and requires only a small power consumption to achieve a high heat supply. There are currently less research on heat pump and DAC devices, and energy coupling is not sufficient. As disclosed in patent document CN115479406a, a carbon-absorbing air source heat pump composite system is disclosed, in which a DAC device is an absorption type, and the heat pump is used to collect the heat of adsorption in the operation process of the DAC device to heat a building. Patent CN115077130B discloses a double-heat source heat pump type air-carbon direct capturing system, which comprises a waste heat recovery system, a high-temperature heat supply heat pump system and air CO 2 A continuous direct capture system. The waste heat source and adsorption heat in the DAC trapping process are utilized to provide a heat source for the high-temperature heat supply pump, so that double heat source supply is realized.
As can be seen from the foregoing, the current DAC technology has many problems in terms of energy utilization and integration:
(1) The higher capture energy consumption of the DAC mainly comes from the heat input during desorption and the cold input during adsorption.
(2) There are many parts of the DAC device that can be used for energy recovery during operation. Such as high temperature sensible heat after desorption, heat released during adsorption, and corresponding required cold, sensible heat of drying air at the adsorption outlet, etc.
The DAC device and the heat pump equipment are combined to remarkably reduce the energy consumption of DAC trapping, but in the current research, only the heat pump equipment is often used for absorbing heat from the DAC equipment, or only the hot end of the heat pump is used for supplying heat for the DAC equipment, so that the utilization of cold end cold energy of the heat pump is ignored, and the efficient utilization of the heat pump equipment is not realized.
Disclosure of Invention
Aiming at the problems and potential optimization measures existing in the prior DAC technology, the invention provides a heat pump driving DAC system and a heat pump driving DAC method for evaporating and cooling treatment gas based on TVSA circulation. The invention further analyzes the links which exist in the circulating process of combining the heat pump with the DAC device and can be used for energy utilization.
The inventor finds that the condenser and the evaporator of the heat pump can provide heat and cold energy for the desorption process and the adsorption process of the DAC system to form high-temperature desorption and precooling/internal cooling adsorption, thereby realizing the efficient utilization of cold and hot double ends of the heat pump system. In the initial stage of adsorption, the high-temperature treatment gas at the outlet stores higher sensible heat, and the part of high-temperature treatment waste gas can provide a heat source for the air source heat pump, so that the evaporation temperature of the heat pump is increased, and the COP of the heat pump is greatly improved. In addition, the invention also discovers that the dry air at the adsorption outlet contains latent heat and cold energy in the adsorption process, and the air is introduced into the evaporative cooler to obtain considerable cooling water which can be used for regenerating H in the gas 2 O is separated, so that the energy recovery and comprehensive utilization efficiency of the DAC device is improved. The invention also adopts a direct heat exchange mode, improves the heat exchange efficiency and reduces the heat exchange dissipation.
A heat pump driven direct air carbon capture system based on TVSA cycle exhaust evaporative cooling is proposed. The system consists of three subsystems, namely an evaporative cooling subsystem, a heat pump subsystem and a DAC subsystem. An evaporative cooler in the evaporative cooling subsystem is thermally connected with a processing pipeline of the DAC subsystem, and latent heat cold in the drying processing waste gas is recovered. The circulation pipeline of the evaporative cooling subsystem is thermally connected with the first condenser of the DAC subsystem and is used for condensing water vapor in the produced gas. The condenser of the heat pump subsystem is thermally connected with the adsorption bed of the DAC subsystem to provide desorption heat for the adsorption bed.
A heat pump driven air direct carbon trapping device based on TVSA circulation comprises an evaporative cooler, a heat pump subsystem and a DAC subsystem mainly composed of at least two adsorption beds and a first condenser;
the heat pump condenser of the heat pump subsystem is connected with heat exchange channels (or medium pipelines) of a plurality of adsorption beds through an internal heat source circulation loop, so that desorption heat is provided for the DAC subsystem;
an air inlet of the evaporative cooler is connected with a processing air pipeline of the DAC subsystem through a pipeline, and the latent heat waste heat of the processing air of the DAC subsystem is recovered; and the gas produced by the DAC subsystem is condensed by connecting the condensation circulation loop with a medium pipeline of the first condenser.
The invention fully utilizes the characteristic of treatment drying, generates a condensation cold source through the evaporative cooler and is used for the condensation process of the first condenser, thereby obviously improving the concentration of produced gas, efficiently recovering the latent heat in the treatment gas and realizing the integral energy integration and optimization of the DAC subsystem.
In one technical scheme, a medium pipeline of the DAC subsystem is connected with a condenser of the heat pump subsystem through a pipeline, and after the medium pipeline is heated by the condenser of the heat pump subsystem, desorption heat is provided for the adsorption bed. In actual connection, the heat exchange tube inside the adsorbent of the DAC subsystem is connected with the inlet pipeline of the heat pump condenser, and the outlet pipeline of the heat pump condenser is respectively connected with the inlets of the inner cold and heat source of the two adsorption beds of the DAC subsystem through the three-way valve to provide desorption heat for the adsorption beds in desorption state.
Preferably, the DAC subsystem has two adsorption beds, namely a first adsorption bed and a second adsorption bed.
As a more specific technical scheme, the internal heat source circulation loop further comprises a hot water tank, a hot water pump, a tenth switching valve and an eleventh switching valve. The outlet of the heat pump condenser is connected with a hot water tank through a heat pump hot water outflow pipe, the hot water tank is connected with a hot water pump through a pipeline, the outlet of the hot water pump is connected with the first end of a tenth switching valve, and the second end and the third end of the tenth switching valve are respectively connected with the inlets of heat exchange channels of the two adsorption beds through pipelines; the inlet of the heat pump condenser is connected with the first end of the eleventh switching valve through a heat pump hot water inflow pipe, and the second end and the third end of the eleventh switching valve are respectively connected with the outlets of the heat exchange channels of the two adsorption beds to form a complete internal heat source circulation loop.
As an implementation mode, the condensation circulation loop further comprises a condensation cold source water tank and a condensation cold source water pump. The evaporative cooler uses the hot gases generated from the DAC subsystem to exchange heat, cool it, and convert it to cooling water. The condensing cold source water tank and the condensing cold source water pump are respectively used for providing a stable condensing cold source for the first condenser and circularly supplying cooling medium.
During the actual connection, the delivery port of evaporative cooler passes through the pipeline and links to each other with condensation cold source water tank, condensation cold source water pump in proper order, and then condensation cold source water pump passes through the pipeline and links to each other with the medium pipeline entry of first condenser, and the export of the medium pipeline of first condenser passes through the pipeline and links to each other with evaporative cooler's water inlet, forms complete condensation circulation loop.
Further, the air inlet of the evaporative cooler is connected with the processing air pipeline of the DAC subsystem through a pipeline, and in actual connection, the processing air outlet pipe of the DAC subsystem and the second air inlet pipe with the switching valve are connected with the air inlet of the evaporative cooler through the air mixing inlet pipe at the same time.
As an embodiment, the treatment gas line is connected to the heat pump evaporator, cooled by the heat pump evaporator, and then connected to the gas inlet of the evaporative cooler. In actual connection, the treatment gas outlet pipe of the DAC subsystem is firstly connected with the refrigerating fluid inlet pipe of the heat pump evaporator through a pipeline, after cold energy is recovered through the heat pump evaporator, the cold energy is discharged through the refrigerating fluid outlet pipe, and then the cold energy is further recovered from the treatment gas through the pipeline and the second air inlet pipe with a switching valve and connected with the air inlet of the evaporative cooler through the air mixing inlet pipe.
As one implementation scheme, the device also comprises a cooling tower, wherein the cooling tower is connected with the heat exchange channels of the adsorption beds through an internal cold source circulation loop, so that adsorption heat generated in the adsorption process is taken away, and adsorption internal cooling is provided for the DAC subsystem. According to the technical scheme, the adsorption internal cooling source is provided for the adsorption bed through the cooling tower. The natural cold source generated by the cooling tower is used as an internal cold source to promote the adsorption process, thereby greatly improving CO 2 The trapping amount of the device reduces the internal cooling energy consumption. In addition to using heatThe evaporator or cooling tower of the pump system can also select other cold sources as internal cold sources to promote the adsorption process according to the requirements.
Further, the internal cold source circulation loop also comprises a cooling water tank and a cooling water pump, cold water generated by the cooling tower is collected by the cooling water tank, and circulation power is provided by the cooling water pump so as to realize cold energy transmission. More specifically, the internal cold source circulation loop further comprises a twelfth switching valve and a thirteenth switching valve, when the internal cold source circulation loop is specifically connected, the outlet pipeline of the cooling water pump is connected with the first end of the twelfth switching valve, the second end and the third end of the twelfth switching valve are respectively connected with the inlets of the heat exchange channels of the two adsorption beds through pipelines, the outlets of the heat exchange channels of the two adsorption beds are respectively connected with the second end and the third end of the thirteenth switching valve through pipelines, and the first end of the thirteenth switching valve is connected with the inlet of the cooling tower through the pipelines, so that the adsorption cold energy is provided for the adsorption beds in an adsorption state.
As an embodiment, the DAC subsystem further comprises a second condenser disposed in series with the first condenser, and the liquid outlet end of the second condenser condensation line is connected to the liquid inlet end of the first condenser condensation line. The produced gas is primarily condensed by the second condenser and then enters the first condenser to be further condensed.
Further, the cooling tower is communicated with the medium pipeline of the second condenser through the primary condensation circulation pipeline; and pre-cooling capacity is provided for the second condenser by using a cooling tower. By adopting the technical scheme, the natural cold source of the cooling tower and the condensation cold source generated by the evaporative cooler are utilized to respectively perform preliminary condensation and deep condensation, so that CO can be effectively improved 2 And reduces overall condensing energy consumption.
Further, the primary condensation circulation pipeline further comprises a cooling water tank and a cooling water pump. When the cooling water pump is connected, the water outlet of the cooling tower is connected with the water inlet of the cooling water tank, the water outlet of the cooling water tank is connected with the cooling water pump, the outlet pipeline of the cooling water pump is connected with the medium pipeline inlet of the second condenser, and the medium pipeline outlet of the second condenser is connected with the water inlet of the cooling tower through a pipeline.
As one embodiment, the heat pump evaporator is connected to the heat exchange channel through an internal cold source circulation loop to provide adsorption internal cooling to the DAC subsystem. By adopting the technical scheme, the heat pump evaporator is utilized to take away the adsorption heat generated in the adsorption process. The cold quantity of the evaporation side of the heat pump can be utilized to perform internal cooling to promote the adsorption process, so that the gas yield is effectively improved. Further, in actual connection, the outlet of the evaporator of the heat pump subsystem is sequentially connected with the cold water tank and the cold water pump through a refrigerating fluid outlet pipe, and then is respectively connected with the inlets of the cooling pipelines of the two adsorption beds of the DAC subsystem through pipelines with three-way valves to provide adsorption cold energy for the adsorption beds; and meanwhile, the inlet of the evaporator of the heat pump subsystem is connected with a refrigerating fluid inlet pipe, and the refrigerating fluid inlet pipe is respectively connected with the outlets of the cooling pipelines of the two adsorption beds through pipelines with three-way valves, so that the circulation of a cold water loop of the heat pump is realized.
As one embodiment, the system further comprises a precooler for precooling inlet air, wherein a precooling pipeline of the precooler is communicated with an air inlet pipe of the DAC subsystem; the heat pump evaporator is connected with a medium pipeline of the precooler through a precooling circulation loop and precools air before entering the adsorption bed. The cold energy of the heat pump system is fully utilized to pre-cool the inlet air so as to reduce the air temperature and the moisture content and effectively improve the CO 2 Collection amount. Furthermore, the precooling circulation loop also comprises a cold water tank and a cold water pump, and the medium pipeline of the heat pump evaporator, the cold water tank and the medium pipeline of the cold water pump and the precooler are sequentially connected to form a precooling heat exchange loop. In actual connection, a fan for air intake is connected with a precooling pipeline inlet of a precooler, and a precooling pipeline outlet pipeline of the precooler is respectively connected with air inlets of two adsorption beds of a DAC subsystem through a pipeline with a three-way valve or is respectively connected with the two adsorption beds through a branch circuit with a switching valve; the evaporator outlet of the heat pump subsystem is respectively connected with the cold water tank and the cold water pump in sequence through a refrigerating fluid outlet pipe, and then is further connected with the medium pipeline inlet of the precooler through a pipeline, and the medium pipeline outlet of the precooler is connected with the evaporator inlet of the heat pump subsystem through a refrigerating fluid inlet pipe.
As an alternative, the heat pump condenser and the heat pump evaporator in the above technical solutions are removed, and the adsorption bed (i.e. the high-temperature adsorption bed) in the desorption state is directly used as the condenser of the heat pump subsystem, and the precooler is used as the evaporator of the heat pump subsystem; and a precooling pipeline of the precooler is communicated with an air inlet pipe of the DAC subsystem.
Further, the heat pump subsystem consists of a compressor, an expansion valve, a heat exchange channel (serving as a condenser) of the high-temperature adsorption bed and a medium pipeline of a precooler. The outlet of the compressor is connected with the inlets of the heat exchange channels of the two adsorption beds through a pipeline with a three-way valve; the inlet of the expansion valve is respectively connected with the outlets of the two adsorption bed heat exchange channels through a pipeline with a three-way valve; the outlet of the expansion valve is connected with the inlet of the medium pipeline of the precooler through a pipeline, and the outlet of the medium pipeline of the precooler is connected with the inlet of the compressor through a pipeline.
As an alternative, the heat pump condenser and the heat pump evaporator in the above technical solutions are removed, the adsorption bed (high-temperature adsorption bed) in the desorption state is directly used as the condenser of the heat pump subsystem to provide the desorption heat required by desorption, and the adsorption bed (low-temperature adsorption bed) in the adsorption state is directly used as the evaporator of the heat pump subsystem to provide the internal cooling source required by adsorption.
As one implementation mode, the device further comprises a four-way valve, the outlet of the compression book is connected with the inlet of the heat exchange channel of the high-temperature adsorption bed through one passage of the four-way valve, the outlet of the heat exchange channel of the high-temperature adsorption bed is connected with the expansion valve, the other end of the expansion valve is connected with the inlet of the heat exchange passage of the low-temperature adsorption bed, the outlet of the heat exchange passage of the low-temperature adsorption bed is connected with the other passage of the four-way valve, and the other end of the passage is connected with the inlet of the compressor. When adsorption-desorption operations are alternately carried out on the adsorption beds, the four-way valve is used for realizing connection with the corresponding adsorption beds.
Further, a bypass branch with a bypass valve is also provided in parallel with the compressor. After the high-temperature adsorption bed finishes desorption and the low-temperature adsorption bed finishes adsorption, the technical scheme can realize the cycle backheating process, realize the preheating of the high-temperature adsorption bed and the cold quantity of the low-temperature adsorption bed, and respectively realize the precooling and the preheating of the two adsorption beds. More specifically, after the high-temperature adsorption bed completes desorption and the low-temperature adsorption bed completes adsorption, the refrigerant in the high-temperature adsorption bed is still in a high-temperature and high-pressure state, and the refrigerant in the low-temperature adsorption bed is still in a low-temperature and low-pressure state; in order to reduce the internal cooling and internal heat energy loss during mode conversion, the system increases the cycle back heating process; in the cycle backheating process, the compressor is firstly closed, and the bypass valve is opened; at the moment, the high-temperature adsorption bed and the low-temperature adsorption bed are directly communicated, and the refrigerants in the two adsorption beds are subjected to a severe mixing process instantly, so that the liquid refrigerant in the high-pressure state in the high-temperature adsorption bed is rapidly evaporated, the heat remained in the desorption process is absorbed, and the high-temperature adsorption bed is pre-cooled; meanwhile, the low-pressure gaseous refrigerant in the low-temperature adsorption bed is rapidly condensed, and simultaneously releases heat to preheat the low-temperature adsorption bed, so that the cycle backheating process is completed.
The DAC subsystem is a core part of the direct air carbon capture system and consists of an adsorption bed, a treatment gas pipeline, a cooling tower and other auxiliary equipment. The adsorption bed adsorbs CO in the air by the adsorbent 2 Realize CO 2 And (5) capturing. The treatment gas pipeline is used for preprocessing the air before entering the adsorption bed, including dehumidification, heating, compression and the like. The cooling tower is used for cooling the heat of adsorption generated during the adsorption process to maintain the operating temperature of the adsorbent bed.
The whole system realizes the heat pump driving direct air carbon trapping process of exhaust gas evaporative cooling by coordinating the operation of the three subsystems. The technical proposal fully utilizes the recovery and the reutilization of heat energy, improves the CO 2 Efficiency of trapping and simultaneously reduced energy consumption and carbon emissions.
As one embodiment, the DAC subsystem consists essentially of:
the first adsorption bed and the second adsorption bed are provided with heat exchange channels and are used for alternately carrying out adsorption and desorption operations;
an air inlet pipe connected with the air inlets of the first adsorption bed and the second adsorption bed respectively;
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 bed and the second adsorption bed, 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.
In the present invention, the chilled fluid of the heat pump evaporator may be derived from ambient air, renewable energy sources, industrial waste heat, and the like. On one hand, the evaporation temperature of the heat pump system can be obviously improved, and the performance of the heat pump system is improved; on the other hand, the device also realizes the efficient recycling of low-grade waste heat resources and improves the overall benefit of the DAC device.
Compared with the prior DAC system, the invention realizes the following technical advantages:
1. the invention adopts a TVSA circulating DAC trapping subsystem, utilizes the evaporative cooling of the vapor in the evaporative cooler to convert the low moisture content potential energy in the drying treatment gas of the adsorption outlet into the cooling capacity of cooling water for desorbing H in the air suction 2 O condensation and separation, thereby realizing high concentration CO 2 Is a result of the production of (2); the DAC is deeply combined with cold and hot double-end energy of the heat pump, the heat pump condenser provides heat for heating the adsorbent in the desorption process of the DAC subsystem, and the evaporator provides cold for precooling or internal cooling in the adsorption process of the DAC subsystem, so that double-end efficient utilization of the heat pump energy is realized, and the operation energy consumption of the DAC subsystem is greatly reduced;
2. the invention uses the evaporative cooler to convert the potential energy of dry air at the adsorption outlet of the DAC subsystem into the energy of cooling water, and is H in the product gas at the desorption outlet of the DAC subsystem 2 The O condensation separation provides cold energy to obtain high-concentration CO 2 Producing gas; the utilization of dry air realizes the recovery transfer and form conversion of energy from the adsorption side to the desorption side in the DAC subsystem, and completes the reduction of high H in the desorption side by the low relative humidity air potential energy of the adsorption side 2 Potential energy conversion of O concentration realizes high-efficiency energy recovery and integrated utilization of the DAC subsystem;
3. the invention realizes the double-end utilization of the heat side and the cold side of the heat pump, greatly improves the cold and hot utilization efficiency of the heat pump subsystem, and effectively reduces the overall energy consumption of the heat pump subsystem;
4. according to the invention, the cold source generated by the evaporator end of the heat pump is introduced into the adsorption bed to realize internal cooling adsorption or pre-cooling air to realize pre-cooling adsorption, so that the adverse effect of adsorption heat on the adsorption process is reduced, and the trapping efficiency and the trapping performance of the DAC subsystem are improved;
5. the invention uses the cooling water generated by the dry air evaporative cooler to 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, sensible heat of outlet treatment gas in the adsorption process is introduced into the heat pump evaporator side for heat recovery, so that the evaporation temperature is increased, the running COP of the heat pump is increased, the recovery and utilization of adsorption heat in the DAC subsystem are realized, the integral energy utilization and integration efficiency of the DAC and heat pump combined system are enhanced, and the overall energy consumption is reduced;
7. According to the invention, the high-efficiency utilization of the heat of the DAC device is realized through the back heating between the double beds in the circulation process, the heat input and cold input requirements are reduced, and the overall operation energy consumption of the device is reduced;
8. 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 a schematic diagram of a heat pump driven air direct carbon capture system based on TVSA in embodiment 1;
fig. 2 is a schematic structural diagram of a TVSA-based heat pump driven air direct carbon capture system in embodiment 2;
fig. 3 is a schematic structural diagram of a TVSA-based heat pump driven air direct carbon capture system in embodiment 3;
fig. 4 is a schematic diagram of a structure of a TVSA-based heat pump driven air direct carbon capture system in embodiment 4;
FIG. 5 is a schematic diagram of a heat pump driven air direct carbon capture system based on TVSA in embodiment 5;
fig. 6 is a schematic structural diagram of a TVSA-based heat pump driven air direct carbon capture system in embodiment 6;
in the figure:
1. fan 17, first compressor 33, precooler
2. First air inlet duct 18, CO 2 Storage cylinder 34, heat pump hot water inflow pipe
3. First switch valve 19, second air inlet pipe 35, heat pump hot water outflow pipe
4. Second switching valve 20, ninth switching valve 36, and hot water tank
5. First adsorption bed 21, air mixing inlet pipe 37 and hot water pump
6. Second adsorbent bed 22, evaporative cooler 38, tenth switching valve
7. Third switching valve 23, exhaust gas discharge pipe 39, eleventh switching valve
8. Fourth switching valve 24, condensing cold source water tank 40, second condenser
9. Fifth switching valve 25, condensing cold source water pump 41 and cooling tower
10. Sixth switching valve 26, heat pump subsystem 42, and cooling water tank
11. Treated gas outlet pipe 27, heat pump evaporator 43, and cooling water pump
12. Seventh switching valve 28, heat pump condenser 44, twelfth switching valve
13. Vacuum pump 29, chilled fluid inlet pipe 45, thirteenth switching valve
14. Vacuum exhaust outlet pipe 30, chilled fluid outlet pipe 46, and second compressor
15. Eighth switching valve 31, cold water tank 47, expansion valve
16. First condenser 32, cold water pump 48, four-way reversing valve
Detailed Description
The following description of the embodiments is made with reference to the accompanying drawings.
Example 1: the hot water of the heat pump condenser is used as an internal heat source for desorption, the cold water of the heat pump evaporator is used as an inlet air precooling cold source, the cooling water of the cooling tower is used as a primary condensation cold source, and the evaporative cooling cold water is used as a deep condensation cold source to be H 2 Condensation of O provides refrigeration.
Referring to fig. 1, a heat pump driven air direct carbon capture device based on TVSA cycle includes an evaporative cooler 22, a heat pump subsystem 26, and a DAC subsystem consisting essentially of a first adsorbent bed 5, a second adsorbent bed 6, and a first condenser 16. The heat pump condenser is connected with heat exchange channels of the first adsorption bed and the second adsorption bed through an internal heat source circulation loop, so that desorption heat is provided for the DAC subsystem; the air inlet pipeline of the evaporative cooler is connected with the processing pipeline of the DAC subsystem through a pipeline, and the cooling capacity in the processing air of the DAC subsystem is recovered; and the gas produced by the DAC subsystem is condensed by connecting the condensation circulation loop with a medium pipeline of the first condenser.
The connection mode is as follows:
in the device, the air inlet of the first adsorption bed 5 is communicated with the first air inlet pipe 2 through the first switching valve 3, and the air outlet is connected to the treatment air outlet pipe 11 through the fifth switching valve 9; the air inlet of the second adsorption bed 6 is communicated with the first air inlet pipe 2 through the second switching valve 4, and the air outlet is also connected to the treatment outlet pipe 11 through the sixth switching valve 10; a fan 1 is mounted at the inlet of the first air inlet duct 2 to drive air into the adsorbent bed.
One end of the third switching valve 7 is connected to a pipeline between the fifth switching valve 9 and the first adsorption bed 5, and the other end is connected to the fourth switching valve 8 through a pipeline; the other end of the fourth switching valve 8 is connected to a line between the sixth switching valve 10 and the second adsorbent bed 6; one end of the seventh switching valve 12 is connected to a line between the third switching valve 7 and the fourth switching valve 8, and the other end is connected to a vacuum exhaust outlet pipe 14 provided with a vacuum pump 13.
One end of the eighth switching valve 15 is connected with the third switch through a pipelineThe pipeline between the change valve 7 and the fourth switching valve 8 is connected, and the other end is connected with the inlet end of the condensation pipeline in the second condenser 40; the outlet end of the condensing pipeline in the second condenser 40 is communicated with the inlet end of the condensing pipeline in the first condenser 16; the outlet end of the condensing pipeline of the first condenser 16 is connected with one end of the first compressor 17, and the other end of the first compressor 17 is connected with CO 2 A gas cylinder 18 is stored.
The heat pump 26 mainly comprises a heat pump evaporator 27, a heat pump condenser 28, and a corresponding compressor and expansion valve.
A frozen fluid outlet pipe 30 on the heat pump evaporator 27 is connected with a water inlet of a cold water tank 31, and a water outlet of the cold water tank 31 is connected with a cold water pump 32; the other end of the cold water pump 32 is connected with the inlet end of the medium pipeline of the precooler 30; the medium line outlet end of the precooler 33 is connected to the heat pump evaporator 27 via a chilled fluid inlet pipe 29.
Air enters a precooling pipeline of a precooler 33 under the driving of a fan 1, and then enters the first adsorption bed 5 or the second adsorption bed 6 through a first switching valve 3 or a second switching valve 4.
The heat pump hot water outflow pipe 35 on the heat pump condenser 28 is connected with the water inlet of the hot water tank 36, and the water outlet of the hot water tank 30 is connected with the hot water pump 37; the other end of the hot water pump 37 is connected to one end of a tenth switching valve 38; the second end and the third end of the tenth switching valve 38 are connected to the medium inlets of the first adsorbent bed 5 and the second adsorbent bed 6, respectively; the second and third ends of the eleventh switching valve 39 are connected to the medium outlets of the first adsorbent bed 5 and the second adsorbent bed 6, and the first end is communicated with the heat pump condenser 28 through the heat pump hot water inflow pipe 34.
The liquid outlet ends of the fifth switching valve 9 and the sixth switching valve 10 are connected with a treated gas outlet pipe 11, the treated gas outlet pipe 11 and a second air inlet pipe 19 with a ninth switching valve 20 are connected with a mixed air inlet pipe 21 together, the other end of the mixed air inlet pipe 21 is connected with an air inlet of an evaporative cooler 22, and an air outlet of the evaporative cooler 22 is connected with an exhaust gas discharge pipe 23 for discharging exhaust gas. The water outlet of the evaporative cooler 22 is sequentially connected with a condensation cold source water tank 24 and a condensation cold source water pump 25 through pipelines, the other end of the condensation cold source water pump 25 is connected with the medium pipeline inlet of the first condenser 16, and the mass pipeline outlet of the first condenser 16 is connected with the water inlet of the evaporative cooler 22 through a pipeline.
The outlet end of cooling water of the cooling tower 41 is connected with the water inlet of the cooling water tank 42, and the water outlet of the cooling water tank 42 is connected with the cooling water pump 43; the other end of the cooling water pump 43 is connected with the medium pipeline inlet end of the second condenser 40; the medium line outlet end of the second condenser 40 is connected from the cooling water inlet end of the cooling tower 41 back to the cooling tower 41.
The working flow is as follows:taking the case where the second adsorbent bed 6 is in the adsorption state and the first adsorbent bed 5 is in the desorption state as an example:
when the second adsorption bed 6 needs to enter an adsorption state, the second switching valve 4 and the sixth switching valve 10 should be opened first, and the first switching valve 3 and the fourth switching valve 8 should be closed; under the drive of the fan 1, air sequentially flows through the first air inlet pipe 2, the precooler 33 and the second switching valve 4 and enters the second adsorption bed 6; the second adsorption bed 6 with the solid adsorbent arranged therein can fully adsorb CO in the inflowing air 2 And H 2 O, and discharges low CO through the sixth switching valve 10 2 A process gas having a low concentration and a low moisture content; the process gas flows along the process gas outlet pipe 11 and is mixed with the air flowing in through the second air inlet pipe 19 and the ninth switching valve 20 in a certain ratio; the mixed air flows into the evaporative cooler 22 through the mixed air inlet pipe 21, takes away the heat of the condensation cold source to cool the condensation cold source rapidly, and then is discharged out of the system through the waste gas discharge pipe 23.
When the first adsorption bed 5 needs to enter a desorption state, the third switching valve 7 and the seventh switching valve 12 are required to be opened, the fifth switching valve 9 and the eighth switching valve 15 are required to be closed, and the vacuum pump 13 is required to be started; the air in the first adsorption bed 5 flows through the third switching valve 7, the seventh switching valve 12 and the vacuum pump 13 in sequence under the driving of the vacuum pump 13, and finally is discharged out of the system from the vacuum exhaust outlet pipe 14; subsequently, the seventh switching valve 12 and the vacuum pump 13 are closed, and the eighth switching valve 15 is opened, so that the desorption gas passes through the third switching valve 7, the eighth switching valve 15, the second condenser 40 and the first condenser 16 in this order; the water vapor contained in the stripping gas is cooled in the second condenser 40 and the first condenser 16Coagulation separation, residual high concentration CO 2 The gas is first compressed in a first compressor 17 and then stored in CO 2 Stored in a gas cylinder 18.
To realize H 2 O and CO 2 An internal heat source line is added to the system to circulate the hot water between the heat pump condenser 28 and the first adsorbent bed 5; at this time, one end of the tenth switching valve 38 and the eleventh switching valve 39 connected to the second adsorbent bed 6 is closed; the heat pump condenser 28 generates hot water using the released condensation heat and discharges it from the heat pump hot water outflow pipe 35; the hot water flows through the hot water tank 36, the hot water pump 37 and the tenth switching valve 38, and finally enters the first adsorption bed 5 as H 2 O and CO 2 Providing heat for desorption of (a); after flowing out of the first adsorption bed 5, the hot water passes through an eleventh switching valve 39 and flows back into the heat pump condenser 28 from the heat pump hot water inflow pipe 34.
To reduce the temperature and moisture content of the inlet air, CO is promoted 2 Adsorption, the system also pre-cools the inlet air; the cold water circulates between the heat pump evaporator 27 and the precooler 33 by the cold water pump 32; cold water flowing out of the heat pump evaporator 27 sequentially passes through the frozen fluid outlet pipe 30, the cold water tank 31 and the cold water pump 32, and finally flows into the precooler 33 through the medium pipeline inlet end of the precooler 33 to pre-cool inlet air; the temperature of the air can be reduced, and part of water vapor in the air can be pre-condensed, so that the adsorption effect of the device is improved; the cold water then flows out of the medium line outlet end of the precooler 33 back into the heat pump evaporator 27 via the chilled fluid inlet tube 29.
The cooling water circulates between the cooling tower 41 and the second condenser 40 by being driven by the cooling water pump 43; the cooling water flows out from the cooling water outlet end of the cooling tower 41, sequentially passes through the cooling water tank 42 and the cooling water pump 43, flows into the second condenser 40 from the medium pipeline inlet end, and promotes H in the produced gas 2 Preliminary condensation of O; subsequently, the cooling water flowing out of the second condenser 40 flows back into the cooling tower 41 from the cooling water inlet end of the cooling tower 41.
The condensation cold source circulates between the evaporative cooler 22 and the first condenser 16 under the drive of the condensation cold source water pump 25; the condensation cold source flowing out from the water outlet of the evaporative cooler 22 flows through the condensation cold source water tank 24 and the condensation cold source water pump 25 in sequence, and finally flows into the first condenser 16 from the medium pipeline inlet end of the first condenser 16, so as to help the product gas to further condense the moisture in the exhaust gas; the condensing cold source then flows out of the first condenser 16, through the water inlet of the evaporative cooler 22, and back into the evaporative cooler 22.
Advantages are:
the embodiment respectively couples and matches the cold quantity and the heat quantity of the cold end and the hot end of the heat pump to the precooling energy consumption and the regeneration energy consumption, thereby realizing the efficient utilization of the cold and hot double-end energy of the heat pump system; the heat pump evaporator is utilized to provide cold energy for the precooler, so that the temperature of inlet air is reduced, a low-temperature environment is provided for the adsorption process, partial vapor in the air can be pre-condensed, and the partial vapor and CO are avoided 2 A competitive adsorption phenomenon occurs during the adsorption process; meanwhile, the natural cold source generated by the cooling tower is utilized to primarily condense the product gas, so that the condensation energy consumption of the system is reduced; introducing the dried treatment gas into an evaporative cooler, and recovering the cooling capacity of the treatment gas and simultaneously recovering H in the product gas 2 The deep condensation of O provides a cold source, and further purification of the product gas is realized.
Example 2: the heat pump condenser takes hot water as an internal heat source to promote desorption, the heat pump evaporator takes cold water as an internal cold source to promote adsorption, the cooling tower cooling water as a primary condensation cold source, and the evaporation cooling cold water as a deep condensation cold source is H 2 Condensation of O provides refrigeration.
Referring to fig. 2, the difference from example 1 is that the heat pump evaporator cold water as an internal cold source is connected to the adsorption bed heat exchange channel. While the precooler of example 1 is removed. In the following description of embodiment 2, reference is made to fig. 1 for the occurrence of numbers omitted from fig. 2, and the corresponding components and the manner of action and connection of the components are referred to in embodiment 1.
The connection mode is as follows:
a frozen fluid outlet pipe 30 on the heat pump evaporator 27 is connected with a water inlet of a cold water tank 31, and a water outlet of the cold water tank 31 is connected with a cold water pump 32; the other end of the cold water pump 32 is connected with the first end of a twelfth switching valve 44, and the second end and the third end of the twelfth switching valve 44 are respectively connected with the medium inlets of the heat exchange channels on the outer walls of the first adsorption bed and the second adsorption bed; the medium outlets of the heat exchange channels of the outer walls of the first adsorption bed and the second adsorption bed are respectively connected with the second port and the third port of the thirteenth switching valve 45, and the first port of the thirteenth switching valve 45 flows back to the heat pump evaporator 27 through the refrigerating fluid inlet pipe 29 to complete the circulation of the internal cold source.
At the air inlet, the fan 1 is used as a drive, the outlet is connected with one ends of the first switching valve 3 and the second switching valve 4 through a first air inlet pipe, and the other ends of the first switching valve 3 and the second switching valve 4 are respectively connected with the air inlets of the first adsorption bed and the second adsorption bed. The remaining connections were the same as in example 1.The working flow is as follows:taking the case where the second adsorbent bed 6 is in the adsorption state and the first adsorbent bed 5 is in the desorption state as an example:
in embodiment 2, the working procedures of the vacuumizing pipeline, the gas generating pipeline, the primary condensation cold source pipeline and the deep condensation cold source pipeline of the system are completely the same as those of embodiment 1, and are not repeated here; the difference of example 2 compared to example 1 is mainly represented in the workflow of the process gas line, the internal heat source line and the internal heat source line.
In the process gas line, the second switching valve 4 and the sixth switching valve 10 should be opened first, and the first switching valve 3 and the fourth switching valve 8 should be closed; under the drive of the fan 1, air sequentially flows through the first air inlet pipe 2 and the second switching valve 4 and enters the second adsorption bed 6; the second adsorption bed 6 is provided with a solid adsorbent which can fully adsorb CO in the air 2 And H 2 O; after the adsorption is completed, the CO is low 2 The process gas of low concentration and low moisture content is discharged from the sixth switching valve 10, flows along the process gas outlet pipe 11, and is mixed with the air flowing in through the second air inlet pipe 19 and the ninth switching valve 20 in a certain ratio; the mixed air flows into the evaporative cooler 22 through the mixed air inlet pipe 21, takes away the heat of the condensation cold source to cool the condensation cold source rapidly, and then is discharged out of the system through the waste gas discharge pipe 23.
In the internal heat source line, the hot water is driven by a hot water pump 37 to circulate between the heat pump condenser 28 and the first adsorbent bed 5; at this time, the end of the tenth switching valve 38 connected to the line between the twelfth switching valve 44 and the second adsorbent bed 6 should be closed, and the end of the eleventh switching valve 39 connected to the line between the thirteenth switching valve 45 and the second adsorbent bed 6 should be closed; the hot water absorbs the condensation heat in the hot water loop inside the heat pump condenser 28, heats up, flows out from the heat pump hot water outflow pipe 35, passes through the hot water tank 36, the hot water pump 37 and the tenth switching valve 38, and finally flows into the first adsorption bed 5 to serve as an internal heat source of the DAC desorption bed to promote desorption; the hot water flowing out of the first adsorption bed 5 flows back into the heat pump condenser 28 from the heat pump hot water inflow pipe 34 through the eleventh switching valve 39.
In the internal cold source line, cold water is driven by a cold water pump 32 to circulate between the heat pump evaporator 27 and the second adsorbent bed 6; at this time, the end of the twelfth switching valve 44 connected to the line between the tenth switching valve 38 and the first adsorbent bed 5 should be closed, and the end of the thirteenth switching valve 45 connected to the line between the eleventh switching valve 39 and the first adsorbent bed 5 should be closed; cold water generated by the heat pump evaporator 27 flows out of the chilled fluid outlet pipe 30, flows through the cold water tank 31, the cold water pump 32 and the twelfth switching valve 44 in sequence, finally flows into the second adsorption bed 6, and takes away adsorption heat generated in the adsorption process; cold water flowing from the second adsorbent bed 6 passes through the thirteenth switching valve 45 and flows back into the heat pump evaporator 27 from the chilled fluid inlet pipe 29.
Advantages are:
this embodiment uses heat from the condensing side of the heat pump to promote CO in DAC system 2 And H 2 O is desorbed, the adsorption bed is internally cooled by utilizing the cold energy of the evaporation side, so that deep energy integration is realized, and the energy utilization efficiency of the heat pump is improved; meanwhile, partial steam is primarily condensed by utilizing a natural cold source of the cooling tower, so that the condensation energy consumption of the system is reduced; in addition, the evaporative cooler is used for generating a condensation cold source for the condensation process of the first condenser, so that the cold energy of the treatment gas is recovered, and the H in the product gas is also recovered 2 The deep condensation of O provides a cold source, and realizes high concentration CO 2 And (5) producing product gas.
Example 3: the heat pump condenser takes hot water as an internal heat source to promote desorption, the heat pump evaporator recovers low-grade waste heat resources, cooling water of a cooling tower is taken as an internal cold source to promote adsorption, and evaporative cooling cold water is taken as a deep condensation cold source to be H 2 Condensation of O provides refrigeration.
Referring to fig. 3, the difference from embodiment 2 is that the internal heat sinks of the first and second adsorption beds are not directly provided by the heat pump evaporator any more, but are provided by an internal heat sink circulation loop composed of a cooling tower 41, a cooling water tank 42, and a cooling water pump 43. At this time, the twelfth switching valve 44 and the thirteenth switching valve 45 are provided in the internal heat sink circulation circuit. And the heat pump evaporator is directly used for recovering low-grade waste heat resources. In addition, in this embodiment, the second condenser and the medium circulation line for one are not provided. Also, in the following description of embodiment 3, reference is made to fig. 1 for the omitted numbers in fig. 3, and the corresponding components and the manner of their function and connection are referred to embodiment 1.
The connection mode is as follows:
the chilled fluid inlet pipe 29 and chilled fluid outlet pipe 30 of the heat pump evaporator are connected to a low-grade waste heat resource recovery system, respectively.
The cooling water outlet of the cooling tower 41 is connected with the water inlet of the cooling water tank 42, the water outlet of the cooling water tank 42 is connected with the cooling water pump 43 through a pipeline, the other end of the cooling water pump 43 is connected with the first end of the twelfth switching valve 44, and the second end and the third end of the twelfth switching valve 44 are respectively connected with the medium pipeline inlets of the first adsorption bed and the second adsorption bed. The medium line outlets of the first and second adsorption beds are connected to the second and third ends of the thirteenth switching valve 45, respectively, and the first end of the thirteenth switching valve 45 is connected to the cooling water inlet of the cooling tower 41.
In actual connection, the third end of the tenth switching valve 38 is connected to the line between the twelfth switching valve 44 and the second adsorbent bed; the third end of the eleventh switching valve 39 is connected to a line between the thirteenth switching valve 45 and the second adsorbent bed; a second end of the twelfth switching valve 44 is connected to the line between the tenth switching valve 38 and the first adsorbent bed, and a second end of the thirteenth switching valve 45 is connected to the line between the eleventh switching valve 39 and the first adsorbent bed.
The working flow is as follows:taking the case where the second adsorbent bed 6 is in the adsorption state and the first adsorbent bed 5 is in the desorption state as an example:
in embodiment 3, the working flows of the treatment gas pipeline, the vacuumizing pipeline, the deep condensation cold source pipeline and the internal heat source pipeline of the system are completely the same as those of embodiment 2, and are not repeated here; the difference of example 3 compared to example 2 is mainly represented in the workflow of the gas generating line, the internal cold source and the heat pump chilled fluid line.
In the gas production line, the seventh switching valve 12 and the vacuum pump 13 should be closed, and the eighth switching valve 15 should be opened to desorb the sucked CO 2 -H 2 The O-mixed gas flows through the third switching valve 7, the eighth switching valve 15, and the first condenser 16 in this order; the water vapor contained in the desorbed gas is condensed and discharged in the first condenser 16, and the residual high concentration CO 2 The gas is introduced into the first compressor 17 for pressurization and then stored in CO 2 Stored in a gas cylinder 18.
In the internal cold source pipeline, the cooling water is driven by the cooling water pump 43 to circularly flow between the cooling tower 41 and the second adsorption bed 6; at this time, the end of the twelfth switching valve 44 connected to the line between the tenth switching valve 38 and the first adsorbent bed 5 should be closed, and the end of the thirteenth switching valve 45 connected to the line between the eleventh switching valve 39 and the first adsorbent bed 5 should be closed; the cooling water flows out from the cooling water outlet end of the cooling tower 41, flows into the second adsorption bed 6 through the cooling water tank 42, the cooling water pump 43 and the twelfth switching valve 44, and is used for taking away the adsorption heat generated in the internal cooling adsorption process, so that adverse effects on the adsorption process are eliminated; the cooling water then flows out of the second adsorbent bed 6, through the thirteenth switching valve 45, and back into the cooling tower 41 from the cooling water inlet end.
In the heat pump refrigerating fluid pipeline, refrigerating fluid enters the heat pump evaporator 27 from the refrigerating fluid inlet pipe 29, and the evaporation temperature of the heat pump evaporator 27 is increased by utilizing waste heat contained in the refrigerating fluid, so that the efficiency of the heat pump 26 is improved; the frozen fluid is then discharged from the frozen fluid outlet pipe 30; the chilled fluid used in this embodiment may be from ambient air, renewable energy, industrial waste heat, and the like.
Advantages are:
the embodiment utilizes the heat of the condensing side of the heat pump to provide an internal heat source for the DAC desorption bed, and simultaneously utilizes the refrigerating fluid from air, industrial waste heat and the like to improve the evaporation temperature of the heat pump, so that the performance of the heat pump is improved, the double-end efficient utilization of the heat pump energy is realized, and the operation benefit of the system is improved; the cooling water generated by the cooling tower is used for providing an internal cold source for the adsorption bed, so that the adverse effect of adsorption heat on the adsorption process is eliminated; in addition, the cold energy of the treatment gas is recovered through the evaporative cooling pipeline and is H in the product gas 2 The deep condensation of O provides a cold source, so that CO can be effectively improved 2 Is a trapping concentration of (a).
Example 4: the heat pump condenser takes hot water as an internal heat source to promote desorption, the heat pump evaporator recovers sensible heat waste heat of treatment gas, and the evaporative cooling cold water is taken as a deep condensation cold source to be H 2 Condensation of O provides refrigeration.
Referring to fig. 4, the differences from embodiment 3 are mainly that: no cooling tower and corresponding internal cold source circulation pipeline are arranged. Meanwhile, the treated gas outlet pipe 11 of the first adsorption bed or the second adsorption bed is not directly connected with the air inlet of the evaporative cooler, but is connected with the refrigerating fluid inlet pipe 29 of the heat pump evaporator, and then is connected with the air inlet of the evaporative cooler after cold energy is recovered by the heat pump evaporator, so that the cold energy in the treated gas is further recovered. Also, in the following description of embodiment 4, reference is made to fig. 1 for the omitted numbers in fig. 4, and the corresponding components and the manner of their function and connection are referred to embodiment 1.
The connection mode is as follows:
the process gas outlet pipe 11 is connected with a refrigerating fluid inlet pipe 29 of the heat pump evaporator through a pipeline, and a refrigerating fluid outlet pipe 30 of the heat pump evaporator is combined with a second air inlet pipe through a pipeline and then is connected with a mixed air inlet pipe, and finally is connected with an air inlet of the evaporative cooler through the mixed air inlet pipe.
The working flow is as follows:taking the case where the second adsorbent bed 6 is in the adsorption state and the first adsorbent bed 5 is in the desorption state as an example:
in embodiment 4, the working flows of the vacuumizing pipeline, the deep condensing cold source pipeline, the gas producing pipeline and the internal heat source pipeline of the system are completely the same as those of embodiment 3, and are not repeated here; the difference of example 4 compared to example 3 is mainly represented in the workflow of the process gas line and the heat pump chilled fluid line.
In the treatment gas pipeline, after the second adsorption bed 6 is adsorbed, the CO content is low 2 The process gas of low concentration and low moisture content is discharged from the sixth switching valve 10, flows along the process gas outlet pipe 11, and enters the heat pump evaporator 27 through the refrigerating fluid inlet pipe 29.
In the heat pump refrigerating fluid pipeline, the processing gas entering the heat pump evaporator 27 from the refrigerating fluid inlet pipe 29 contains higher sensible heat, so that a heat source can be provided for the air source heat pump, and the evaporation temperature of the heat pump system is increased; the process gas whose temperature has been lowered is discharged from the refrigerating fluid outlet pipe 30 and mixed with the air flowing in through the second air inlet pipe 19 and the ninth switching valve 20 in a certain ratio; the mixed air flows into the evaporative cooler 22 through the mixed air inlet pipe 21, absorbs the heat of the condensing cold source to cool the condensing cold source, and then is discharged out of the system through the exhaust gas discharge pipe 23.
Advantages are:
this embodiment uses heat from the condensing side of the heat pump to provide an internal heat source for the DAC desorber while using low CO 2 Low H 2 The high-temperature treatment gas with the O content provides a heat source for the air source heat pump, so that sensible heat of the treatment gas is fully recycled, and the performance of the heat pump and the operation benefit of the system are improved; meanwhile, an evaporative cooling loop is arranged in the system, low-temperature treatment gas discharged by the heat pump evaporator is utilized to provide cold energy for a condensation cold source, and H in gas production is promoted 2 O condensation, facilitating improvement of CO of the system 2 Product gas concentration and comprehensive energy utilization efficiency.
Example 5: adopts a direct heat exchange mode, and the refrigerant at the condensation side of the heat pump is used as internal heatThe source promotes desorption, the refrigerant on the evaporation side of the heat pump is used as an inlet air precooling cold source to promote adsorption, and the evaporative cooling cold water is used as a deep condensation cold source to be H 2 Condensation of O provides refrigeration.
Referring to fig. 5, the gas outlets of the first adsorbent bed 5 and the second adsorbent bed 6 are connected in a similar manner to example 1 except for the gas producing line, see example 1. The main difference is that in the gas producing section, only one condenser, i.e. the first condenser 16, is provided in this embodiment, and no second condenser or the like is provided. The independent condenser and the evaporator are removed from the heat pump subsystem, the heat pump subsystem is directly connected with the first adsorption bed or the second adsorption bed through a pipeline, and the refrigerant is utilized to directly provide desorption heat for the adsorption beds, so that the precooling of air is realized. Also, in the following description of embodiment 5, reference is made to fig. 1 for the omitted numbers in fig. 5, and the corresponding components and the manner of their function and connection are referred to embodiment 1.
The connection mode is as follows:
the outlet of the compressor 46 is connected to the first end of the tenth switching valve 38 through a pipeline, and the second end and the third end of the tenth switching valve 38 are respectively connected to the medium pipeline inlets of the first adsorbent bed 5 and the second adsorbent bed 6. The medium pipeline outlets of the first adsorption bed 5 and the second adsorption bed 6 are respectively connected with the second end and the third end of the eleventh switching valve 39 through pipelines, the first end of the eleventh switching valve 39 is connected with the inlet end of the expansion valve 47 through a pipeline, the outlet end of the expansion valve 47 is connected with the inlet of a precooler medium pipeline through a pipeline, and the outlet of the precooler medium pipeline is connected with the inlet of a compressor through a pipeline. The fan is connected with a first air inlet pipe which is connected with air inlets of the first adsorption bed and the second adsorption bed through a precooler through pipelines with a first switching valve and a second switching valve respectively.
The gas-generating section-related piping is the same as in examples 3 and 4, see examples 3 and 4.
The working flow is as follows:taking the case where the second adsorbent bed 6 is in the adsorption state and the first adsorbent bed 5 is in the desorption state as an example:
in embodiment 5, the working flows of the processing gas pipeline, the vacuumizing pipeline and the deep condensing cold source pipeline of the system are completely the same as those of embodiment 1, and are not repeated here; the difference of example 5 compared to example 1 is mainly in the gas production line and the connection of the DAC adsorbent bed to the heat pump system, thereby changing the workflow of example 5.
In the gas production line, the seventh switching valve 12 and the vacuum pump 13 should be closed, and the eighth switching valve 15 should be opened to desorb the sucked CO 2 -H 2 The O mixed gas sequentially passes through a third switching valve 7, an eighth switching valve 15 and a first condenser 16; the water vapor contained in the desorbed gas is condensed and discharged in the first condenser 16, and the residual high concentration CO 2 The gas is introduced into the first compressor 17 for pressurization and then stored in CO 2 Stored in a gas cylinder 18.
The workflow change caused by the change of the connection mode of the DAC adsorption bed and the heat pump system is embodied as the conversion of the indirect heat exchange mode into the direct heat exchange mode. In the direct heat exchange process, one end, connected with the second adsorption bed 6, of the tenth switching valve 38 and the eleventh switching valve 39 should be closed first; the high-temperature and high-pressure refrigerant gas generated by the second compressor 46 flows out from the outlet end of the second compressor 46, passes through the tenth switching valve 38 and enters the first adsorption bed 5; the refrigerant gas condenses in the first adsorption bed 5 and releases a large amount of condensation heat, so that the DAC desorption process is promoted to be smoothly carried out; the condensed refrigerant flows out of the first adsorption bed 5, enters the expansion valve 47 through the eleventh switching valve 39, becomes a refrigerant in a low-temperature and low-pressure state, flows from the expansion valve 47 to the medium pipeline inlet end of the precooler 33, precools the inlet air, reduces the temperature and the moisture content of the air, and promotes CO 2 Is an adsorption process of (a); the refrigerant then flows from the media line outlet end of precooler 33 to second compressor 46.
Advantages are:
in the embodiment, an evaporator and a condenser in the heat pump subsystem are directly replaced by a precooler and a desorption bed in the DAC subsystem, desorption is promoted through condensation heat release of high-temperature and high-pressure refrigerant, a pre-cooling source is provided through evaporation heat absorption of low-temperature and low-pressure refrigerant, and CO is obtained through the method 2 And H 2 The adsorption and desorption of O create a suitable environment; meanwhile, the refrigerant is utilized to directly exchange heat, so that the energy loss caused by heat exchange between the refrigerant and other media is avoided, the condensation temperature of the heat pump subsystem can be effectively reduced, and the evaporation temperature of the heat pump subsystem can be improved, and the efficiency of the heat pump subsystem and the overall performance of the device are greatly improved; in addition, the cold energy in the dry treatment gas is recovered through the evaporative cooling pipeline and is H in the product gas 2 The deep condensation of O provides a cold source, which not only reduces the condensation energy consumption, but also greatly improves the CO 2 Concentration of product gas.
Example 6: the heat pump condensation side refrigerant is used as an internal heat source to promote desorption, the heat pump evaporation side refrigerant is used as an internal cold source to promote adsorption, cooling water of a cooling tower is used as a primary condensation cold source, and the evaporation cooling cold water is used as a deep condensation cold source to be H 2 The condensation of O provides cold and adopts a circulation back-heating scheme.
Referring to fig. 6, the main difference from embodiment 5 is that the adsorption bed in the adsorption state in the DAC subsystem acts as an evaporator of the heat pump subsystem; the adsorption bed in the desorbed state acts as a condenser for the heat pump subsystem; a bypass branch with a fourteenth switching valve 49 is also connected in parallel to the branch of the compressor 46; a four-way reversing valve 48 is also provided. Meanwhile, the second condenser and the corresponding primary condensation circulation loop arranged on the basis of the embodiment 5 can be used for specific connection modes and the like, and can be seen in the embodiment 1 or the embodiment 2.
The working flow is as follows:taking the case where the second adsorbent bed 6 is in the adsorption state and the first adsorbent bed 5 is in the desorption state as an example:
in embodiment 6, the working procedures of the treatment gas pipeline, the vacuumizing pipeline, the gas production pipeline, the primary condensation cold source pipeline and the deep condensation cold source pipeline of the system are identical to those of embodiment 2, and are not repeated here; the difference of example 6 compared to example 2 is mainly in the connection of the DAC adsorbent bed to the heat pump system, thereby enabling a change in the workflow of example 6.
The workflow change caused by the change of the connection mode of the DAC adsorption bed and the heat pump system is embodied as the conversion of the indirect heat exchange mode into the direct heat exchange mode. In the direct way In the heat exchange process, the fourteenth switching valve 49 is closed firstly, and the four-way reversing valve 48 is adjusted to enable the refrigerant outlet end of the second compressor 46 to be connected with one end of the medium pipeline of the first adsorption bed 5, and the refrigerant inlet end of the second compressor 46 is connected with one end of the medium pipeline of the second adsorption bed 6; the high-temperature high-pressure refrigerant gas generated by the second compressor 46 flows out from the outlet end, passes through the four-way reversing valve 48 and enters the first adsorption bed 5; the refrigerant gas condenses in the first adsorbent bed 5 to release heat, which is CO 2 And H 2 Desorption of O provides sufficient heat; then the refrigerant flows from the first adsorption bed 5 to the expansion valve 47, becomes low-temperature low-pressure refrigerant in the expansion valve 47, is sent into the second adsorption bed 6, creates a low-temperature environment for the adsorption process of the DAC system, and improves the adsorption efficiency of the system; the refrigerant flowing from the second adsorbent bed 6 is returned to the second compressor 46 via the four-way reversing valve 48.
After the first adsorption bed 5 finishes desorption and the second adsorption bed 6 finishes adsorption, the refrigerant in the first adsorption bed 5 is still in a high-temperature and high-pressure state, and the refrigerant in the second adsorption bed 6 is still in a low-temperature and low-pressure state; in order to reduce the internal cooling and internal heat energy loss during mode conversion, the system increases the cycle back heating process; during the cycle regeneration, the second compressor 46 should first be turned off and the fourteenth switching valve 49 opened; at this time, the first adsorbent bed 5 and the second adsorbent bed 6 are directly communicated through the four-way reversing valve 48 and the fourteenth switching valve 49, and the refrigerants in the two adsorbent beds instantaneously undergo a severe mixing process, so that the liquid refrigerant in the first adsorbent bed 5 in a high-pressure state is rapidly evaporated, the heat remaining in the desorption process is absorbed, and the first adsorbent bed 5 is pre-cooled; at the same time, the low-pressure gaseous refrigerant in the second adsorption bed 6 is rapidly condensed and simultaneously releases heat to preheat the second adsorption bed 6, thereby completing the cycle regenerative process.
After the circulation back heating is completed, the corresponding passage is adjusted through the four-way reversing valve 48, so that the inlet of the compressor is connected with the heat exchange passage of the second adsorption bed which is about to enter the desorption state to provide desorption heat; the outlet of the first adsorption bed heat exchange passage which is about to enter the adsorption state is connected with the inlet of the compressor, so as to provide adsorption cooling.
Advantages are:
in the embodiment, an evaporator and a condenser in the heat pump subsystem are directly replaced by an adsorption bed and a desorption bed in the DAC subsystem, a second compressor is utilized to generate high-temperature and high-pressure refrigerant, the desorption bed is heated by means of the condensation heat release process to promote desorption, a low-temperature and low-pressure refrigerant is generated by an expansion valve to provide a cold source for the adsorption bed, and a low-temperature environment is created for condensation of water vapor; the refrigerant is utilized to directly exchange heat, so that the energy loss caused by heat exchange between the refrigerant and other media is avoided, the condensation temperature of the heat pump subsystem can be effectively reduced, and the evaporation temperature of the heat pump subsystem can be improved, thereby greatly improving the efficiency of the heat pump subsystem and the overall performance of the device; meanwhile, the cold source provided by the cooling tower and the evaporative cooler is used for primary condensation and deep condensation, so that the condensation energy consumption is reduced, and the CO is also improved 2 Is a trapping concentration of (1); in addition, through the circulation backheating process, the aim of preheating the adsorption bed and precooling the desorption bed is fulfilled by utilizing the pressure difference of the refrigerant after the reaction is finished, thereby being beneficial to reducing the condensation and regeneration energy consumption of the system and improving the comprehensive energy utilization efficiency of the system.
Claims (10)
1. The heat pump driven air direct carbon trapping device based on TVSA circulation is characterized by comprising an evaporative cooler, a heat pump subsystem and a DAC subsystem which mainly comprises at least two adsorption beds and a first condenser;
the heat pump condenser of the heat pump subsystem is connected with heat exchange channels of a plurality of adsorption beds through an internal heat source circulation loop, so that desorption heat is provided for the DAC subsystem;
an air inlet of the evaporative cooler is connected with a processing air pipeline of the DAC subsystem through a pipeline, and the latent heat waste heat of the processing air of the DAC subsystem is recovered; and the gas produced by the DAC subsystem is condensed by connecting the condensation circulation loop with a medium pipeline of the first condenser.
2. The TVSA cycle based heat pump driven air direct carbon capture device of claim 1, wherein said process gas line is connected to a heat pump evaporator prior to cooling thereof and then to the inlet of said evaporative cooler.
3. The TVSA cycle based heat pump driven air direct carbon capture device of claim 1, further comprising a cooling tower connected to the heat exchange channels of the plurality of adsorbent beds through an internal cold source circulation loop for providing adsorption internal cooling to the DAC subsystem.
4. The TVSA cycle based heat pump driven air direct carbon capture device of claim 1, wherein said DAC subsystem further comprises a second condenser disposed in series with the first condenser, and wherein the liquid outlet end of the second condenser condensing conduit is connected to the liquid inlet end of the first condenser condensing conduit.
5. The TVSA cycle based heat pump driven air direct carbon capture device of claim 4, further comprising a cooling tower in communication with the medium line of the second condenser through a preliminary condensation cycle line.
6. The TVSA cycle based heat pump driven air direct carbon capture device of claim 1, wherein said heat pump evaporator is connected to said heat exchange channel through an internal cold source circulation loop to provide adsorption internal cooling to the DAC subsystem.
7. The TVSA cycle based heat pump driven air direct carbon capture device of claim 1, further comprising a precooler having a precooling line in communication with an air inlet tube of said DAC subsystem; the heat pump evaporator is connected with a medium pipeline of the precooler through a precooling circulation loop and precools air before entering the adsorption bed.
8. The TVSA cycle based heat pump driven air direct carbon capture device of any one of claims 1, 2, 4, 5, 7, wherein said adsorbent bed in a desorbed state directly acts as a condenser of said heat pump subsystem and a precooler acts as an evaporator of said heat pump subsystem; and a precooling pipeline of the precooler is communicated with an air inlet pipe of the DAC subsystem.
9. The TVSA cycle based heat pump driven air direct carbon capture device of any one of claims 1, 2, 4, 5, 6, wherein said adsorbent bed in a desorbed state directly acts as a condenser of said heat pump subsystem and said adsorbent bed in an adsorbed state directly acts as an evaporator of said heat pump subsystem.
10. The TVSA cycle based heat pump driven air direct carbon capture device of claim 1, wherein said DAC subsystem consists essentially of:
the first adsorption bed and the second adsorption bed are provided with heat exchange channels and are used for alternately carrying out adsorption and desorption operations;
an air inlet pipe connected with the air inlets of the first adsorption bed and the second adsorption bed respectively;
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 bed and the second adsorption bed, 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.
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