Cooling-heat-electricity-fuel-oxygen cogeneration system

Abstract

A cold-heat-electricity-fuel-oxygen cogeneration system, comprising: a carbon capture module, an energy storage module and a fuel preparation module, wherein: the carbon capture module captures carbon dioxide, absorbs the heat of the heat storage tank during the desorption process and outputs the carbon dioxide to the energy storage module and the fuel preparation module respectively; the energy storage module compresses carbon dioxide during the charging process and stores the compression heat of the compression process, and outputs electric energy to the fuel preparation module or the power grid during the discharge process; the fuel preparation module obtains high-temperature water vapor and high-temperature carbon dioxide using the heat of the electric heater and the electrolysis product, and uses the electric energy output by the energy storage module and the valley power for electrolysis, and outputs the heat energy to the carbon capture module and the energy storage module respectively; in the charging and discharging process, according to the needs of the fuel preparation module for carbon dioxide at different pressures, carbon dioxide at different pressures is output from the energy storage module to the fuel preparation module for fuel preparation. The present invention improves energy utilization efficiency through multi-energy complementarity, and realizes the cogeneration of cold, heat, electricity, fuel, oxygen and other products based on carbon dioxide.

Description

Technical Field

[0001] The present invention relates to a technology in the field of energy storage and chemical synthetic fuel, specifically a cold-heat-electricity-fuel-oxygen cogeneration system. Background Art

[0002] The characteristics and shortcomings of existing cogeneration technologies include: using clean energy for power supply, mainly cogeneration of heat and power, improving the overall efficiency of energy utilization through the synergy of heat and electricity, enhancing the stability and reliability of energy supply, reducing dependence on a single energy source, and reducing pollution to the environment. At present, the newly proposed cogeneration technologies are all based on cogeneration of heat and power, and the system is improved to cogeneration of cooling, heat and power or cogeneration of heat and electricity. The flexibility of the energy provided to the outside needs to be improved. Summary of the invention

[0003] The present invention aims to solve the problem that the existing direct air carbon capture technology, liquid carbon dioxide energy storage technology and SOEC technology do not fully utilize the electric energy and thermal energy in each link, and are unable to organically control the cooling supply and comprehensively adjust the output ratios of cooling, heat, electricity, fuel and oxygen due to geographical restrictions. The present invention proposes a cooling-heat-electricity-fuel-oxygen cogeneration system, which improves energy utilization efficiency through multi-energy complementarity and realizes the cogeneration of cooling, heat, electricity, fuel, oxygen and other products based on carbon dioxide.

[0004] The present invention is achieved through the following technical solutions:

[0005] The present invention relates to a cold-heat-electricity-fuel-oxygen cogeneration system, comprising: a carbon capture module, an energy storage module and a fuel preparation module, wherein: the carbon capture module captures carbon dioxide, absorbs heat from a heat storage tank during a desorption process and outputs the carbon dioxide to the energy storage module and the fuel preparation module respectively; the energy storage module compresses carbon dioxide and stores compression heat during a charging process, and outputs electric energy to the fuel preparation module or a power grid during a discharging process; the fuel preparation module obtains high-temperature water vapor and high-temperature carbon dioxide using heat from an electric heater and electrolysis products, performs electrolysis using electric energy output from the energy storage module and off-peak electricity, and outputs heat energy to the carbon capture module and the energy storage module respectively; during the charging and discharging process, according to the fuel preparation module's need for carbon dioxide at different pressures, carbon dioxide at different pressures is output from the energy storage module to the fuel preparation module for fuel preparation.

[0006] The carbon capture module comprises: a blower, a carbon dioxide adsorption unit, a carbon dioxide desorption unit and a vacuum pump which are connected in sequence.

[0007] The energy storage module includes: a first heat exchanger, a first condenser, a second heat exchanger, a low-pressure carbon dioxide storage tank, a throttle valve, a third heat exchanger, a carbon dioxide compression pressure regulating device, a second condenser, a high-pressure carbon dioxide storage tank, a centrifugal pump, a carbon dioxide expansion pressure regulating device, a heat exchange fluid unit, a heat storage tank, a cold exchange fluid unit and a cold storage tank connected in sequence.

[0008] The carbon dioxide compression and pressure regulating device comprises: first to n-stage compressors, first to n-stage compression heat exchangers, and a plurality of pressure sensors and valves.

[0009] The carbon dioxide expansion and pressure regulating device comprises: first to n-stage expansion heat exchangers, first to n-stage expanders, first to n-1-stage cold storage heat exchangers, and a plurality of pressure sensors, temperature sensors and valves.

[0010] The fuel preparation module includes: a high-temperature solid oxide electrolysis cell, a fourth heat exchanger, a fifth heat exchanger and a methanation reactor.

[0011] The high-temperature solid oxide electrolytic cell comprises: an air blower, an air preheat exchanger, a first electric heater and an electrolytic cell anode connected in sequence, a carbon dioxide blower, a carbon dioxide preheat exchanger, a mixer, a second electric heater and an electrolytic cell cathode connected in sequence, and a water pump, a steam generator, and a steam preheat exchanger connected in sequence.

[0012] The present invention uses intelligent energy management technology and large-scale cross-season and cross-regional energy storage technology to improve energy utilization efficiency through multi-energy complementarity under different system operation modes, and realizes the co-production of cold, heat, electricity, fuel, oxygen and other products based on carbon dioxide, meeting the future demand for energy diversification. It is a future-oriented, efficient, comprehensive and intelligent energy management technology. BRIEF DESCRIPTION OF THE DRAWINGS

[0013] Figure 1 It is a schematic diagram of the system of the present invention;

[0014] Figure 2 This is a schematic diagram of a carbon capture module of the present invention;

[0015] Figure 3 This is a schematic diagram of the energy storage module of the present invention;

[0016] Figure 4 This is a schematic diagram of the carbon dioxide compression and pressure regulating device of the present invention;

[0017] Figure 5 This is a cross-sectional schematic diagram of the position distribution of the carbon dioxide compression and pressure regulating device of the present invention;

[0018] Figure 6 This is a schematic diagram of the carbon dioxide expansion and pressure regulating device of the present invention;

[0019] Figure 7 This is a cross-sectional schematic diagram of the position distribution of the carbon dioxide expansion and pressure regulating device of the present invention;

[0020] Figure 8 This is a schematic diagram of a fuel preparation module of the present invention;

[0021] Fig. 9 This is a schematic diagram of a high temperature solid oxide electrolytic cell of the present invention;

[0022] Fig.10 This is a schematic diagram of the cooling, heating and electricity supply mode;

[0023] Fig.11 It is a schematic diagram of the system carbon dioxide compression and pressure regulating device in the two-stage compression and two-stage expansion mode of cold, heat and electricity supply;

[0024] Fig.12 It is a schematic diagram of the system carbon dioxide compression and expansion device in the two-stage compression and two-stage expansion mode of cold, heat and electricity supply;

[0025] Fig.13 This is a schematic diagram of the fuel and oxygen supply mode;

[0026] Fig.14 The effect of co-electrolysis conversion rate on system efficiency under fuel oxygen supply mode;

[0027] Fig.15 This is a schematic diagram of the combined supply mode of cooling, heating, electricity, fuel and oxygen;

[0028] Fig.16 The effect of compression and expansion stages on round-trip efficiency in the combined heat, electricity, fuel and oxygen power generation mode;

[0029] Fig.17 The influence of compression and expansion stages on the overall efficiency of the system in the combined heat, cooling, electricity, fuel and oxygen power generation mode;

[0030] In the figure: blower 1, carbon dioxide adsorption unit 2, carbon dioxide desorption unit 3, vacuum pump 4, first heat exchanger 5, first condenser 6, second heat exchanger 7, low-pressure carbon dioxide storage tank 8, throttle valve 9, third heat exchanger 10, carbon dioxide compression pressure regulating device 11, second condenser 12, high-pressure carbon dioxide storage tank 13, centrifugal pump 14, carbon dioxide expansion pressure regulating device 15, heat exchange fluid unit 16, heat storage tank 17, cold exchange fluid unit 18, cold storage tank 29, high-temperature solid oxide electrolysis cell 20, fourth heat exchanger 21, fifth heat exchanger 22, methanation reactor 23, first-stage compressor 1101A, first-stage compression heat exchanger 1101B, second-stage compressor 1102A, second-stage compression heat exchanger 1102B , n-1th stage compressor 11n-1A, n-1th stage compression heat exchanger 11n-1B, nth stage compressor 11nA, nth stage compression heat exchanger 11nB, first stage pressure sensor 11P1, second stage pressure sensor 11P2, n-1th stage pressure sensor 11Pn-1, nth stage pressure sensor 11Pn, valves 11V1, 11V1A, 11V1B, 11V1C, 11V2, 11V2A, 11V2B, 11V2C, 11Vn-1, 11Vn-1A, 11Vn-1B, 11Vn-1C, 11Vn, 11VnA, 11VnC, 15V1, 15V1A, 15V1B, 15V1C, 15V1D, 15V1E, 15V1 F, 15V2, 15V2A, 15V2B, 15V2C, 15V2D, 15V2E, 15V2F, 15Vn-1, 15Vn-1A, 15Vn-1B, 15Vn-1C, 15Vn-1D, 15Vn-1E, 15Vn-1F, 15Vn, 15VnA, 15VnC, 15V001, 15V002, 15V003, first stage expansion heat exchanger 1501A, first stage expansion machine 1501B, first stage cold storage heat exchanger 1501C, second stage expansion heat exchanger 1502A, second stage expansion machine 1502B, second stage cold storage heat exchanger 1502C, n-1 stage expansion heat exchanger 15n-1A, n-1 stage expansion machine 15n-1B, n-1th stage cold storage heat exchanger 15n-1C, nth stage expansion heat exchanger 15nA, nth stage expander 15nB, first stage temperature sensor 15T1, second stage temperature sensor 15T2, n-1th stage temperature sensor 15Tn-1, temperature sensor 15T001, first stage pressure sensor 15P1, second stage pressure sensor 15P2, n-1th stage nth stage pressure sensor 15Pn-1, nth stage pressure sensor 15Pn, air blower 2001, air preheat exchanger 2002, first electric heater 2003, carbon dioxide blower 2004, carbon dioxide preheat exchanger 2005, water pump 2006, steam generator 2007, steam preheat exchanger 2008, mixer 2009,The second electric heater 2010, the high temperature solid oxide electrolysis cell anode 2011, the high temperature solid oxide electrolysis cell electrolyte 2012, and the high temperature solid oxide electrolysis cell cathode 2013. DETAILED DESCRIPTION

[0031] like Figure 1-Figure 9 As shown, this embodiment relates to a new fuel production system combining carbon capture, liquid carbon dioxide energy storage and SOEC, including: a carbon capture module, an energy storage module and a fuel preparation module, wherein: the carbon dioxide output end of the carbon capture module is respectively connected to the energy storage module and the fuel preparation module, the electric energy output end of the energy storage module is respectively connected to the fuel preparation module and the power grid, and the thermal energy output end of the fuel preparation module is respectively connected to the carbon capture module and the energy storage module.

[0032] like Figure 2 As shown, the carbon capture module comprises: a blower 1, a carbon dioxide adsorption unit 2, a carbon dioxide desorption unit 3 and a vacuum pump 4 connected in sequence, wherein: the input end of the carbon dioxide desorption unit 3 is respectively connected to the heat exchange fluid unit 16, the heat storage tank 17 and the vacuum pump 4 of the energy storage module, and the vacuum pump 4 is connected to the hot side inlet end of the first heat exchanger 5 of the energy storage module and the high-temperature solid oxide electrolysis cell carbon dioxide blower 2004.

[0033] like Figure 3As shown, the energy storage module includes: a first heat exchanger 5, a first condenser 6, a second heat exchanger 7, a low-pressure carbon dioxide storage tank 8, a throttle valve 9, a third heat exchanger 10, a carbon dioxide compression pressure regulating device 11, a second condenser 12, a high-pressure carbon dioxide storage tank 13, a centrifugal pump 14, a carbon dioxide expansion pressure regulating device 15 and a heat exchange fluid unit 16, a heat storage tank 17, a cold exchange fluid unit 18 and a cold storage tank 19, wherein: the hot side outlet end, the cold side inlet end and the cold side outlet end of the first heat exchanger 5 are respectively connected to the first condenser 6, the heat exchange fluid unit 16 and the heat storage tank 17, the hot side outlet end, the cold side inlet end and the cold side outlet end of the second heat exchanger 7 are respectively connected to the low-pressure carbon dioxide storage tank 8, the cold storage tank 19 and the cold exchange fluid unit 18, the cold side outlet end, The hot side inlet and the hot side outlet are respectively connected to the inlet of the first-stage compressor 1101A, the cold exchange fluid unit 18, and the cold storage tank 19; the outlet of valve 11V001 is connected to the second condenser 12; the outlets of valves 11V1C, 11V2C, 11Vn-1C, and 11VnC are connected to the carbon dioxide blower 2004 of the high-temperature solid oxide electrolysis cell; the centrifugal pump 14 is connected to the cold side inlet of the first-stage expansion heat exchanger 1501A; the outlet of valve 15V001 is connected to the hot side inlet of the first heat exchanger 5; the outlet of valve 15V002 is connected to the hot side inlet of the second heat exchanger 7; the outlets of valves 15V1C, 15V2C, 15Vn-1C, 15VnC, and 15V003 are connected to the carbon dioxide blower 2004 of the high-temperature solid oxide electrolysis cell.

[0034] like Figure 4As shown, the carbon dioxide compression and pressure regulating device comprises: a first-stage compressor 1101A, a first-stage pressure sensor 11P1, a valve 11V1, a first-stage compression heat exchanger 1101B, a valve 11V1B, a second-stage compressor 1102A, a second-stage pressure sensor 11P2, a valve 11V2, a second-stage compression heat exchanger 1102B, a valve 11V2B, an n-1th stage compressor 11n-1A, an n-1th stage pressure sensor 11Pn-1, and a valve 11Vn-1 , n-1 stage compression heat exchanger 11n-1B, valve 11Vn-1B, n stage compressor 11nA, n stage pressure sensor 11Pn, valve 11Vn, n stage compression heat exchanger 11nB, valve 11VnA, valve 11V001 and valve 11V1A, valve 11V1C, valve 11V2A, valve 11V2C, valve 11Vn-1A, valve 11Vn-1C, valve 11VnC, wherein: the first to n stage compression heat exchangers 1101B, 1102B, 11n-1B, 11n The cold side inlet and cold side outlet of B are respectively connected to the heat exchange fluid unit 16 and the heat storage tank 17, the inlet ends of valves 11V1A, 11V2A, and 11Vn-1A are respectively connected to the hot side outlet ends of the first to n-1th stage compression heat exchangers 1101B, 1102B, and 11n-1B, and the outlet ends are connected to the inlet end of valve 11V001, and the inlet ends of valves 11V1C, 11V2C, 11Vn-1C, and 11Vn-1C are respectively connected to the outlet ends of the first stage pressure sensors 11P1, 11P2, 11Pn-1, and 11Pn.

[0035] like Figure 5 As shown, the carbon dioxide compression and pressure regulating device is divided into the first to third layers from top to bottom, the first to nth stage compressors 1101A, 1102A, 11n-1A, 11nA, valves 11V1A, 11V2A, 11Vn-1A, 11VnA, 11V1B, 11V2B, 11Vn-1B, 11V001, the first inlet and the first outlet are located on the first layer of the device, the first to nth stage compression heat exchangers 1101B, 1102B, 11n-1B, 11nB, valves 11V1, 11V2, 11Vn-1, 11Vn, 11V1C, 11V2C, 11Vn-1C, 11VnC, the first stage pressure sensors 11P1, 11P2, 11Pn-1, 11Pn, the second inlet and the third outlet are located on the second layer of the device, and the second outlet is located on the third layer of the device.

[0036] like Figure 6As shown, the carbon dioxide expansion and pressure regulating device comprises: a first-stage expansion heat exchanger 1501A, a first-stage pressure sensor 15P1, a valve 15V1, a first-stage expander 1501B, a valve 15V1B, a first-stage temperature sensor 15T1, a valve 15V1D, a first-stage cold storage heat exchanger 1501C, a valve 15V1F, a second-stage expansion heat exchanger 1502A, a second-stage pressure sensor 15P2, a valve 15V2, a second-stage expander 1502B, a valve 15V2B, a second-stage temperature sensor 15T2, a valve 15V2D, a first-stage cold storage heat exchanger 1502C, a valve 15V2F, an n-1st-stage expansion heat exchanger 15 n-1A, n-1th stage n-1 pressure sensor 15Pn-1, valve 15Vn-1, n-1th stage expander 15n-1B, valve 15Vn-1B, n-1th stage temperature sensor 15Tn-1, valve 15Vn-1D, n-1th stage cold storage heat exchanger 15n-1C, valve 15Vn-1F, n-1th stage expansion heat exchanger 15nA, n-1th stage pressure sensor 15Pn, valve 15Vn, n-1th stage expander 15nB, valve 15VnA, temperature sensor 15T001 and valves 15V1A, valve 15V1C, valve 15V1E, valve 15V2A, valve 15V2C, valve 15V2E, valve 15 Vn-1A, valve 15Vn-1C, valve 15Vn-1E, valve 15VnC, valve 15V001, valve 15V002, valve 15V003, wherein: the hot side inlet and hot side outlet of the first to n-th stage expansion heat exchangers 1501A, 1502A, 15n-1A, 15nA are respectively connected to the heat storage tank 17 and the heat exchange fluid unit 16, the hot side inlet and hot side outlet of the first to n-1 stage cold storage heat exchangers 1501C, 1502C, 15n-1C are respectively connected to the cold exchange fluid unit 18 and the cold storage tank 19, and the inlet of valves 15V1A, 15V2A, 15Vn-1A is respectively connected to the first to n-1 stage expansion machine 1 The outlet ends of 501B, 1502B, and 15n-1B are connected, and the outlet ends are connected to the inlet end of the temperature sensor 15T001. The inlet ends of valves 15V1C, 15V2C, 15Vn-1C, and 15VnC are connected to the outlet ends of the first-stage pressure sensors 15P1, 15P2, 15Pn-1, and 15Pn respectively. The inlet end of valve 15V001 is connected to the outlet end of the temperature sensor 15T001, and the outlet end is connected to the inlet end of the hot side of the first heat exchanger 5. The inlet end of valve 15V002 is connected to the outlet end of the temperature sensor 15T001, and the outlet end is connected to the inlet end of the hot side of the second heat exchanger 7. The inlet end of valve 15V003 is connected to the outlet end of valve 15VnA.

[0037] like Figure 7As shown, the carbon dioxide expansion and pressure regulating device is divided into the first to fourth layers from top to bottom, the first to nth stage expansion machines 1501B, 1502B, 15n-1B, 15nB, valves 15V1A, 15V2A, 15Vn-1A, 15VnA, 15V1B, 15V2B, 15Vn-1B, 15V001, 15V002, 15V003, temperature sensor 15T001, the first outlet, the second outlet are located on the first layer of the device, the first to n-1th stage cold storage heat exchangers 1501C, 1502C, 15n-1C, valves 15V1D, 15V1E, 15V1F, 15V2D, 15V2 E, 15V2F, 15Vn-1D, 15Vn-1E, 15Vn-1F, the first stage temperature sensor 15T1, 15T2, 15Tn-1, the third inlet and the fifth outlet are located on the second layer of the device, the first to nth stage expansion heat exchangers 1501A, 1502A, 15n-1A, 15nA, the first stage pressure sensor 15P1, 15P2, 15Pn-1, 15Pn, valves 15V1, 15V2, 15Vn-1, 15Vn, 15V1C, 15V2C, 15Vn-1C, 15VnC, the first inlet, the second inlet and the fourth outlet are located on the third layer of the device, and the third outlet is located on the fourth layer of the device.

[0038] like Figure 8 As shown, the fuel preparation module includes: a high-temperature solid oxide electrolysis cell 20, a fourth heat exchanger 21, a fifth heat exchanger 22 and a methanation reactor 23, wherein: the high-temperature solid oxide electrolysis cell 20 is connected to a vacuum pump 4, a carbon dioxide compression pressure regulating device 11, a carbon dioxide expansion pressure regulating device 15, a fourth heat exchanger 21, and a fifth heat exchanger 22; the cold side inlet end and the cold side outlet end of the fourth heat exchanger 21 are respectively connected to a heat exchange fluid unit 16 and a heat storage tank 17; the hot side outlet end, the cold side inlet end, and the cold side outlet end of the fifth heat exchanger 22 are respectively connected to a methanation reactor 23, a heat exchange fluid unit 16, and a heat storage tank 17; and the methanation reactor 23 is connected to a heat exchange fluid unit 16 and a heat storage tank 17.

[0039] like Fig. 9As shown, the high temperature solid oxide electrolytic cell 20 comprises: an air blower 2001, an air preheat exchanger 2002, a first electric heater 2003 and an electrolytic cell anode 2011 connected in sequence, a carbon dioxide blower 2004, a carbon dioxide preheat exchanger 2005, a mixer 2009, a second electric heater 2010 and an electrolytic cell cathode 2013 connected in sequence, and a water pump 2006, a steam generator 2007, and a steam preheat exchanger 2008 connected in sequence, wherein: the air blower The machine 2001 is connected to the ambient air and the cold side inlet of the air preheat exchanger 2002. The cold side outlet, hot side inlet and hot side outlet of the air preheat exchanger 2002 are respectively connected to the first electric heater 2003, the anode 2011 of the high-temperature solid oxide electrolysis cell and the hot side inlet of the steam generator 2007. The first electric heater 2003 is connected to the anode 2011 of the high-temperature solid oxide electrolysis cell. The carbon dioxide blower 2004 is connected to the outlet of the vacuum pump 4 of the carbon capture module and the valve 11V1 of the energy storage module. The outlet ends of 11V003, 11V2C, 11Vn-1C, 11VnC, 15V1C, 15V2C, 15Vn-1C, 15VnC and 15V003 are connected; the cold side inlet end, cold side outlet end, hot side inlet end and hot side outlet end of the carbon dioxide preheat exchanger 2005 are connected to the carbon dioxide blower 2004, the mixer 2009, the cathode 2013 of the high temperature solid oxide electrolysis cell and the hot side inlet end of the steam preheat exchanger 2008 respectively; the water pump 2006 is connected to the ambient water and steam generator The cold side inlet end of the steam generator 2007 is connected, the cold side outlet end and the hot side inlet end of the steam generator 2007 are respectively connected to the steam preheat exchanger 2008 and the hot side outlet end of the air preheat exchanger 2002, the cold side outlet end and the hot side inlet end of the steam preheat exchanger 2008 are respectively connected to the mixer 2009 and the hot side outlet end of the carbon dioxide preheat exchanger 2005, the mixer 2009 is connected to the second electric heater 2010, and the second electric heater 2010 is connected to the cathode 2013 of the high-temperature solid oxide electrolysis cell.

[0040] The heat storage tank 17 is filled with heat storage material.

[0041] The cold storage tank 19 is filled with cold storage material.

[0042] The electric energy required by the high-temperature solid oxide electrolysis cell 20 can be provided by valley power or green electricity generated by expanders 1502, 1505, 1508, and 1511 at each stage.

[0043] The present embodiment relates to a cold-heat-electricity-fuel-oxygen cogeneration method based on the above-mentioned system, which respectively implements a cold-heat-electricity supply mode, a fuel-oxygen supply mode, and a cold-heat-electricity-fuel-oxygen multi-energy cogeneration mode according to the load demand of the power grid and the energy demand conditions around the system.

[0044] The said based on the grid load demand and the system's surrounding energy conditions means: when the grid load is low, the charging stage of the cold, heat and electricity supply mode and the cold, heat and electricity, fuel and oxygen multi-energy supply mode is carried out; when the grid load is high, the discharging stage of the cold, heat and electricity supply mode and the cold, heat and electricity, fuel and oxygen multi-energy supply mode is carried out; when the system's surrounding energy has a high demand for cold, heat and electricity and the provided cold, heat and electricity can meet the demand, the cold, heat and electricity supply mode is adopted; when the system's surrounding energy has a low demand for cold, heat and electricity, the fuel and oxygen supply mode is adopted; when the system's surrounding energy has a high demand for cold, heat and electricity and the provided cold, heat and electricity is far greater than the surrounding demand, the cold, heat and electricity, fuel and oxygen multi-energy supply mode is adopted.

[0045] like Fig.10As shown, the cold, heat and electricity supply mode refers to: during the charging process, the liquid carbon dioxide in the low-pressure carbon dioxide storage tank 8 is converted into gas-liquid two-phase coexisting carbon dioxide through the throttle valve 9, and then the cold is released in the third heat exchanger 10 to generate gaseous carbon dioxide, and in the carbon dioxide compression and pressure regulating device 11, the valves 11V1C, 11V2C, 11Vn-1C, and 11VnC are closed, and the valve 11V001 is opened. When the i-th level is required, i≤n, the valves 11ViA and 11V1B to 11Vi-1B are opened among the valves 11V1A to 11VnA and the valves 11V1B to 11Vn-1B, and the remaining valves are closed. Among the valves 11V1 to 11Vn, the front valve 11V1 is opened. i-level valve, close subsequent valves, use low-peak electricity to drive the first to i-level compressors 1101A to 11iA to compress carbon dioxide into a high-temperature and high-pressure supercritical carbon dioxide state, and store the compression heat in the heat storage tank 17 through the first to i-level compression heat exchangers 1101B to 11iB, and finally condense the carbon dioxide into high-pressure liquid carbon dioxide through the second condenser 12 and store it in the high-pressure carbon dioxide storage tank 13; during the discharge process, the liquid carbon dioxide in the high-pressure carbon dioxide storage tank 13 enters the carbon dioxide expansion and pressure regulating device 15 under the action of the centrifugal pump 14, and closes valves 15V1C, 15V2C, 15Vn-1C, 15VnC, and 15V003. When the number of stages is j, j≤n, among valves 15V1A to 15VnA and valves 15V1B to 15Vn-1B, valves 15VjA and 15V1B to 15Vj-1B are opened, and the remaining valves are closed. Among valves 15V1 to 15Vn, the valves of the first j stages are opened, and the subsequent valves are closed. Carbon dioxide is added to the first to j-th stage expansion heat exchangers 1501A to 15jA to absorb the heat stored in the heat storage tank 17, and then enters the first to j-th stage expansion machines 1501B to 15jB in the form of high-temperature and high-pressure carbon dioxide to generate electricity and do work. The carbon dioxide at the outlet of the first to j-1-th stage expansion machines is measured by the corresponding first-stage temperature sensors 15T1 to 15Tj-1 Temperature, for example, the carbon dioxide at the outlet of the k-th expansion machine 15kB is lower than room temperature, k≤j-1, then open valves 15VkD and 15VkF, close valve 15VkE, and store its cold energy in the cold storage tank 19. The carbon dioxide at the outlet of the j-th expansion machine 15jB is measured by the temperature sensor 15T001. If the temperature is higher than room temperature, it is passed into the first heat exchanger 5 to store the heat in the heat storage tank, and then passed into the first condenser 6 to condense to room temperature, and then passed into the second heat exchanger 7. If the temperature is lower than room temperature, it is directly passed into the second heat exchanger 7. The carbon dioxide absorbs the cold energy in the cold storage tank 19 in the second heat exchanger 7 and becomes liquid carbon dioxide stored in the low-pressure carbon dioxide storage tank 8.

[0046] like Fig.13As shown, the fuel oxygen supply mode refers to: after the outside air enters the carbon capture module, it enters the carbon dioxide adsorption unit 2 through the blower 1, and the carbon dioxide therein is adsorbed by the carbon dioxide adsorption unit 2, and then flows into the carbon dioxide desorption unit 3 to desorb high-purity carbon dioxide under the action of the high-temperature heat exchange fluid at the outlet of the heat storage tank 17, and then uses the vacuum pump 4 to desorb under vacuum conditions. The carbon dioxide at the outlet of the vacuum pump 4 is all introduced into the carbon dioxide blower 2004 of the high-temperature solid oxide electrolysis cell 20, and the room temperature air enters the air preheat exchanger 2002 through the air blower 2001, and is preheated by the oxygen at the outlet of the anode 2011 of the high-temperature solid oxide electrolysis cell, and then is heated to 800°C by the first electric heater 2003 and introduced into the anode 2011 of the high-temperature solid oxide electrolysis cell. The carbon dioxide at the outlet of the vacuum pump 4 of the carbon capture module enters the carbon dioxide preheat exchanger 2005 under the action of the carbon dioxide blower 2004, and is used to heat the cathode 201 of the high-temperature solid oxide electrolysis cell. The synthesis gas at the outlet 3 is preheated and then passed into the mixer 2009. The ambient water enters the steam generator 2007 under the action of the water pump 2006, absorbs the heat of the oxygen flowing through the air preheat exchanger 2002, and then enters the steam preheat exchanger 2008. It is preheated by the heat of the synthesis gas flowing through the carbon dioxide preheat exchanger 2005, and then passed into the mixer 2009 to mix with the preheated carbon dioxide, and then heated to 800°C by the second electric heater 2010 and passed into To the cathode 2013 of the high-temperature solid oxide electrolysis cell. The high-temperature solid oxide electrolysis cell 20 is powered by off-peak electricity or external renewable energy. The oxygen and synthesis gas at the outlet of the anode 2011 and the cathode of the high-temperature solid oxide electrolysis cell are respectively introduced into the fourth heat exchanger 21 and the fifth heat exchanger 22 after releasing part of the heat. The oxygen at the outlet of the fourth heat exchanger 21 can be stored or directly used in the oxygen-rich combustion process. The synthesis gas at the outlet of the fifth heat exchanger 22 is introduced into the methanation reactor 23 for methanation reaction to produce fuel.

[0047] like Fig.15As shown, the cold, heat, electricity, fuel and oxygen multi-energy cogeneration mode means that after the outside air enters the carbon capture module, it enters the carbon dioxide adsorption unit 2 through the blower 1, and the carbon dioxide therein is adsorbed by the carbon dioxide adsorption unit 2, and then flows into the carbon dioxide desorption unit 3 to desorb high-purity carbon dioxide under the action of the high-temperature heat exchange fluid at the outlet of the heat storage tank 17, and then uses the vacuum pump 4 to desorb under vacuum conditions, and part of the carbon dioxide at the outlet of the vacuum pump 4 is passed into the first heat exchanger 5 to provide heat to the energy storage module, and part of it is passed into the high-temperature solid oxide In the carbon dioxide blower 2004 of the electrolytic cell 20; during the charging process, the cooled liquid carbon dioxide is stored in the low-pressure carbon dioxide storage tank 8, and the liquid carbon dioxide in the low-pressure carbon dioxide storage tank 8 is converted into carbon dioxide in which gas and liquid coexist through the throttle valve 9, and then the cold energy is released in the third heat exchanger 10 to generate gaseous carbon dioxide, and the valve 11V001 is opened in the carbon dioxide compression and pressure regulating device 11, and when the i-th level is required, the valves 11Vi+1C to 11VnC are closed in the valves 11V1C to 11VnC, and the valve 11V1 Open valve 11ViA and valve 11V1B to 11Vi-1B among valves A to 11VnA and valves 11V1B to 11Vn-1B, close the other valves, open the first i-stage valve among valves 11V1 to 11Vn, close the subsequent valves, use valley power to drive the first to i-stage compressors 1101A to 11iA to compress carbon dioxide into a high-temperature and high-pressure supercritical carbon dioxide state, and store the compression heat in the heat storage tank 17 through the first to i-stage compression heat exchangers 1101B to 11iB, and the heat at the outlet of each stage of the compressor is The first-stage pressure sensors 11P1 to 11Pi are used to detect the compressor outlet pressure. For example, if the x-stage compressor outlet pressure meets the carbon dioxide pressure required in the fuel preparation module at this time, x≤i, then only valve 11VxC is opened among valves 11V1C to 11ViC, and the other valves are closed, and the carbon dioxide under the pressure is introduced into the fuel preparation module to participate in fuel preparation. The carbon dioxide at the outlet of valve 11V001 is condensed into high-pressure liquid carbon dioxide through the second condenser 12 and stored in the high-pressure carbon dioxide storage tank 13;During the discharge process, the liquid carbon dioxide in the high-pressure carbon dioxide storage tank 13 enters the carbon dioxide expansion pressure regulating device 15 under the action of the centrifugal pump 14. When j levels are required, open the valve 15V003, close the valves 15Vj+1C to 15VnC among the valves 15V1C to 15VnC, open the valves 15VjA and 15V1B to 15Vj-1B among the valves 15V1A to 15VnA and the valves 15V1B to 15Vn-1B, close the remaining valves, and open the first j-level valves among the valves 15V1 to 15Vn. The subsequent valves are closed, and carbon dioxide is added to the first to jth expansion heat exchangers 1501A to 15jA to absorb the heat stored in the heat storage tank 17. The first-stage pressure sensors 15P1 and 15Pj at the outlets of the expansion heat exchangers of each stage are used to detect the pressure at the outlet. For example, if the outlet pressure of the yth-stage expansion heat exchanger meets the carbon dioxide pressure required in the fuel preparation module at this time, y≤j, then only valve 15VyC is opened among valves 15V1C to 15VjC, and the other valves are closed, and the carbon dioxide under the pressure is introduced into the fuel preparation module to participate in the combustion. The carbon dioxide at the outlet of each stage of expansion heat exchanger enters the first to j-th stage expansion machines 1501B to 15jB in the form of high-temperature and high-pressure carbon dioxide to generate electricity and perform work. The carbon dioxide at the outlet of the first to j-1-th stage expansion machines is measured by the corresponding first-stage temperature sensors 15T1 to 15Tj-1. For example, the carbon dioxide at the outlet of the k-th stage expansion machine 15kB is lower than the room temperature, k≤j-1, then the valves 15VkD and 15VkF are opened, and the valve 15VkE is closed to store its cold energy in the cold storage tank 19. The j-th stage expansion machine 15jB At the outlet, the net carbon dioxide added by the energy storage module during the charging and discharging process is introduced into the fuel preparation module to participate in the subsequent fuel preparation process. The temperature of the remaining carbon dioxide is measured by the temperature sensor 15T001. If the temperature is higher than the room temperature, it is introduced into the first heat exchanger 5 to store the heat in the heat storage tank, and then introduced into the first condenser 6 to condense to room temperature, and then introduced into the second heat exchanger 7. If the temperature is lower than the room temperature, it is directly introduced into the second heat exchanger 7. The carbon dioxide absorbs the cold energy in the cold storage tank 19 in the second heat exchanger 7 and becomes liquid carbon dioxide and is stored in the low-pressure carbon dioxide storage tank 8. ;

[0048] Normal temperature air enters the air preheat exchanger 2002 through the air blower 2001, is preheated by the oxygen at the outlet of the high temperature solid oxide electrolysis cell anode 2011, and is then heated to 800°C by the first electric heater 2003 and passed into the high temperature solid oxide electrolysis cell anode 2011. The carbon dioxide at the outlet of the carbon capture module vacuum pump 4, the carbon dioxide compression pressure regulating device 11, and the carbon dioxide expansion pressure regulating device 15 enters the carbon dioxide preheat exchanger 2005 under the action of the carbon dioxide blower 2004, is preheated by the synthesis gas at the outlet of the high temperature solid oxide electrolysis cell cathode 2013, and is then passed into the mixer 2009. Ambient water enters the steam generator 2007 under the action of the water pump 2006, absorbs the heat of the oxygen flowing through the air preheat exchanger 2002, and then enters the steam preheat exchanger 2008. The heat of the synthesis gas in the carbon dioxide preheat exchanger 2005 is used to preheat the synthesis gas, and then it is introduced into the mixer 2009 to mix with the preheated carbon dioxide, and then it is heated to 800°C by the second electric heater 2010 and introduced into the cathode 2013 of the high-temperature solid oxide electrolysis cell. The high-temperature solid oxide electrolysis cell 20 is powered by off-peak electricity, external renewable energy and energy storage module. The oxygen and synthesis gas at the outlet of the anode 2011 and cathode of the high-temperature solid oxide electrolysis cell are introduced into the fourth heat exchanger 21 and the fifth heat exchanger 22 respectively after releasing part of the heat, and then part of the heat is stored in the heat storage tank 17. The oxygen at the outlet of the fourth heat exchanger 21 can be stored or directly used in the oxygen-rich combustion process. The synthesis gas at the outlet of the fifth heat exchanger 22 is introduced into the methanation reactor 23 for methanation reaction to produce fuel, and the heat released by the methanation reaction is stored in the heat storage tank 17.

[0049] After simulation calculation, in the cold, heat and electricity supply mode, a two-stage compression and two-stage expansion system was selected for calculation. The ambient pressure was 0.1MPa, the ambient temperature was 25°C, the isentropic efficiency of the compressor, expander and pump was 85%, the heat exchange fluid was 2MPa water, the cold exchange fluid was 1MPa R134a, the temperature of the heat exchange / cold fluid was 25°C, the low-pressure tank pressure was 1.13MPa, the carbon dioxide storage temperature was -43.32°C, the tank volume was 8.96m3, the high-pressure tank pressure was 24.84MPa, the carbon dioxide temperature was 30°C, the tank volume was 10.99m3, the charging time and the discharging time were both 6h, and the carbon dioxide mass flow rate inside the energy storage module was 1687.5kg / h. The number of compression stages in the charging process is 2. At this time, i=2 in the carbon dioxide compression and pressure regulating device. The inlet temperature of the two-stage compressor is 35°C. Open valves 11V2A and 11V1B in valves 11V1A to 11VnA and valves 11V1B to 11Vn-1B, close the remaining valves, open 11V1 and 11V2 in valves 11V1 to 11Vn, close the subsequent valves, and use low-valley electricity to drive the first and second stage compressors 1101A and 1102A to compress carbon dioxide into high-temperature and high-pressure supercritical carbon dioxide. In the carbon dioxide state, the outlet temperatures are 183.90°C and 203.33°C, respectively, and the outlet pressures are 4.26MPa and 24.84MPa, respectively, and the compression heat is stored in the heat storage tank 17 through the first and second stage compression heat exchangers 1101B and 1102B; the discharge process expansion stage is 2, at this time j=2 in the carbon dioxide expansion pressure regulating device, open valve 15V2A and valve 15V1B in valves 15V1A to 15VnA and valves 15V1B to 15Vn-1B, and close the rest Valve, among valves 15V1 to 15Vn, open valves 15V1 and 15V2, close the subsequent valves, and add carbon dioxide to the first and second stage expansion heat exchangers 1501A and 1502A to absorb the heat stored in the heat storage tank 17 to 172.82°C, and then enter the first and second stage expansion machines 1501B and 1502B in the form of high-temperature and high-pressure carbon dioxide to generate electricity and do work. At this time, the temperature of carbon dioxide at the outlet of the first stage expansion machine 1501B is 45.21°C, which is higher than the room temperature. Open valve 15V1E , close valves 15V1D and 15V1F, the temperature of carbon dioxide at the outlet of the second-stage expander is 61.20℃, which is higher than the room temperature, open valve 15V001, close valve 15V002, and pass it into the first heat exchanger 5 to store the heat in the heat storage tank, then pass it into the first condenser 6 to condense to room temperature, and then pass it into the second heat exchanger 7. The carbon dioxide absorbs the cold energy in the cold storage tank 19 in the second heat exchanger 7 and becomes liquid carbon dioxide stored in the low-pressure carbon dioxide storage tank 8. At this time, the round-trip efficiency of the system is 62.33%.

[0050] After simulation calculation, in the fuel oxygen supply mode, the carbon capture module captures carbon dioxide at a scale of 5.624kg / h and passes it all into the fuel preparation module. The electrolysis temperature of the high-temperature solid oxide electrolysis cell in the fuel preparation module is 800℃, the current density is 0.3A / cm2, and the reaction temperature of the methanation reactor is 250℃. Starting the device with a co-electrolysis conversion rate of 90%, the methane production can be 1.85kg / h, the oxygen production is 7.35kg / h, and the total energy efficiency is 81.13%.

[0051] After simulation calculation, in the combined heat, electricity, fuel and oxygen supply mode, the carbon capture module captures carbon dioxide at a scale of 5.624kg / h, and enters the energy storage module and the fuel preparation module at a ratio of 1:1. The ambient pressure is 0.1MPa, the ambient temperature is 25℃, the isentropic efficiency of the compressor, expander and pump is 85%, the heat exchange fluid is 2MPa water, the cold exchange fluid is 1MPa R134a, the temperature of the heat exchange / cold fluid is 25℃, the low-pressure storage tank pressure is 1.13MPa, and the carbon dioxide The storage temperature is -43.32℃, the tank volume is 8.98m3, the high-pressure tank pressure is 24.84MPa, the carbon dioxide temperature is 30℃, the tank volume is 11.00m3, the charging time and discharge time are both 6h, the original carbon dioxide mass flow rate inside the energy storage module is 1687.5kg / h, the electrolysis temperature of the high-temperature solid oxide electrolyzer in the fuel preparation module is 800℃, the current density is 0.3A / cm2, the co-electrolysis conversion rate is 90%, and the reaction temperature of the methanation reactor is 250℃. Select a one-stage compression and one-stage expansion system. The compression stage number of the charging process is 1. At this time, i=1 in the carbon dioxide compression and pressure regulating device, and the inlet temperature of the first-stage compressor is 30°C. Close valves 11V2C to 11VnC in valves 11V1C to 11VnC, open valve 11V1A in valves 11V1A to 11VnA and valves 11V1B to 11Vn-1B, close the remaining valves, open 11V1 in valves 11V1 to 11Vn, close subsequent valves, and use low-valley electricity to drive the first-stage compressor 1101A to compress carbon dioxide into a high-temperature and high-pressure supercritical carbon dioxide state. The outlet temperature is 391.31°C and the pressure is 24.84MPa. At this time, carbon dioxide at this pressure is not needed in the fuel preparation module, so valve 11V1C is closed, and then the first-stage compression heat exchanger 1101B is used. The compression heat is stored in the heat storage tank 17. The carbon dioxide captured by carbon capture is passed into the energy storage module at 2.812 kg / h to perform the energy storage process with the original carbon dioxide inside the energy storage module, and is passed into the fuel preparation module at 2.812 kg / h to perform co-electrolysis with high-temperature steam to produce fuel; the expansion level of the discharge process is 1, at this time, j=1 in the carbon dioxide expansion and pressure regulating device, in valves 15V1C to 15VnC, valves 15V2C to 15VnC are closed, valves 15V1A to 15VnA and valves 15V1B to 15Vn-1B are opened, and the other valves are closed. In valves 15V1 to 15Vn, valve 15V1 is opened, and the subsequent valves are closed. Carbon dioxide is added to the first-stage expansion heat exchanger 1501A to absorb the heat stored in the heat storage tank 17 to 378.78°C, and the pressure is 25.92MPa, at this time, the fuel preparation module does not need carbon dioxide of this pressure, so the valve 15V1C is closed, and then it enters the first-stage expander 1501B in the form of high-temperature and high-pressure carbon dioxide to generate electricity and do work. At this time, the first-stage expander 1501B outlet will pass the net increase of carbon dioxide 2.812kg / h in the energy storage module during the charging and discharging process into the fuel preparation module to participate in the subsequent fuel preparation process. The temperature of the remaining carbon dioxide is 115.48℃, which is higher than the room temperature, so the valve 15V001 is opened, the valve 15V002 is closed, and it is passed into the first exchange The heat is stored in the heat storage tank in the heat exchanger 5, and then passed into the first condenser 6 to condense to room temperature, and then passed into the second heat exchanger 7. The carbon dioxide absorbs the cold energy in the cold storage tank 19 in the second heat exchanger 7 and becomes liquid carbon dioxide stored in the low-pressure carbon dioxide storage tank 8. The 5.624kg / h of carbon dioxide captured by the carbon capture module at this time merges with the carbon dioxide at the outlet of the first-stage expansion machine 1501B, and is passed into the fuel preparation module under the action of the carbon dioxide blower 2004 at a scale of 8.436kg / h for the fuel preparation process. At this time, the best The highest round-trip efficiency is 70.30%; a 14-stage compression and a 5-stage expansion system is selected. The number of compression stages in the charging process is 14. At this time, i=14 in the carbon dioxide compression and pressure regulating device. The inlet temperature of the first to fourteenth stage compressors is 35°C. In valves 11V1C to 11VnC, valves 11V15C to 11VnC are closed. In valves 11V1A to 11VnA and valves 11V1B to 11Vn-1B, valves 11V14 and valves 11V1B to 11V13B are opened. The remaining valves are closed. In valves 11V1 to 11Vn, 1 is opened. 1V1 to 11V14, close the subsequent valves, use the valley power to drive the first to fourteenth compressors 1101A to 1114A to compress the carbon dioxide into a high-temperature and high-pressure supercritical carbon dioxide state, with outlet temperatures of 45.28°C, 55.77°C, 55.84°C, 55.92°C, 56.02°C, 56.13°C, 56.22°C, 56.23°C, 55.90°C, 53.95°C, 41.29°C, 40.31°C, 40.32°C, 40.62°C, and pressures of 0.94MPa, 1.21 MPa, 1.55 MPa, 2.00 MPa, 2.57 MPa, 3.31 MPa, 4.26 MPa, 5.48 MPa, 7.05 MPa, 9.07 MPa, 11.67 MPa, 15.01 MPa, 19.31 MPa, 24.84 MPa. At this time, the fuel preparation module does not need the above pressure of carbon dioxide, so the valves 11V1C to 11V14C are closed, and then the compression heat is stored in the heat storage tank 17 through the first to fourteenth stage compression heat exchangers 1101B to 1114B. The carbon dioxide captured by the carbon capture is 2.812kg / h is introduced into the energy storage module to carry out the energy storage process with the original carbon dioxide inside the energy storage module, and 2.812kg / h is introduced into the fuel preparation module to carry out co-electrolysis with high-temperature water vapor to produce fuel; the expansion level of the discharge process is 5, at this time j=5 in the carbon dioxide expansion pressure regulating device, in valves 15V1C to 15VnC, valves 15V6C to 15VnC are closed, in valves 15V1A to 15VnA and valves 15V1B to 15Vn-1B, valves 15V5A and valves 15V1B to 15V4B are opened, and the remaining valves are closed. In valves 15V1 to 15Vn, valves 15V1 to 15V5 are opened, and subsequent valves are closed, and carbon dioxide is added to the first to fourth stage expansion heat exchangers. 1501A absorbs the heat stored in the heat storage tank 17 to 50.45°C, and the pressures are 25.92MPa, 13.85MPa, 7.40MPa, 3.96MPa, and 2.11MPa, respectively. At this time, the fuel preparation module does not need carbon dioxide at the above pressures, so valves 15V1C to 15V5C are closed, and then it enters the first to fourth stage expanders 1501B to 1504B in the form of high-temperature and high-pressure carbon dioxide to generate electricity and do work. At this time, the temperature of carbon dioxide at the outlet of the first stage expander 1501B is 37.31°C, which is higher than the room temperature. Valve 15V1E is opened, valves 15V1D and 15V1F are closed, and the temperature of carbon dioxide at the outlet of the second stage expander 1502B is 31 .04℃ higher than room temperature, open valve 15V2E, close valves 15V2D and 15V2F, the temperature of carbon dioxide at the outlet of the third-stage expander 1503B is 5.45℃ lower than room temperature, close valve 15V3E, open valves 15V3D and 15V3F, store the cold in the cold storage tank 19 in the third-stage cold storage heat exchanger 1503C, the temperature of carbon dioxide at the outlet of the fourth-stage expander 1504B is 8.70℃ lower than room temperature, close valve 15V4E, open valves 15V4D and 15V4F, store the cold in the cold storage tank 19 in the fourth-stage cold storage heat exchanger 1504C, and the net increase of carbon dioxide 2.812 in the energy storage module during the charging and discharging process is stored at the outlet of the fifth-stage expander 1505B kg / h is passed into the fuel preparation module to participate in the subsequent fuel preparation process. The temperature of the remaining carbon dioxide is 11.46℃, which is lower than the room temperature. Therefore, valve 15V001 is closed and valve 15V002 is opened to pass it into the second heat exchanger 7. The carbon dioxide absorbs the cold energy in the cold storage tank 19 in the second heat exchanger 7 and becomes liquid carbon dioxide stored in the low-pressure carbon dioxide storage tank 8. The 5.624kg / h of carbon dioxide captured by the carbon capture module at this time merges with the carbon dioxide at the outlet of the fifth-stage expansion machine 1505B, and is passed into the fuel preparation module at a scale of 8.436kg / h under the action of the carbon dioxide blower 2004 for the fuel preparation process. At this time, the highest total energy efficiency of 109.75% can be obtained. .

[0052] Compared with the prior art, the present invention can select the cold, heat, electricity supply mode, the fuel and oxygen supply mode, and the cold, heat, electricity, fuel and oxygen multi-energy supply mode according to external energy demand. When operating in the cold, heat, electricity and fuel multi-energy modes, the heat and electricity generated by each module are comprehensively utilized to improve the round-trip efficiency and total energy efficiency of the system, which can reach up to 70.30% and 109.75% respectively.

[0053] In summary, the present invention can be flexibly sited and can flexibly adjust the output energy structure according to the energy demand of the construction site. At the same time, the carbon capture module, the energy storage module, and the fuel preparation module are combined to output carbon dioxide at different pressures for co-electrolysis according to demand, and the cold, heat, and electricity generated inside each module are comprehensively utilized, thereby reducing energy loss and improving the overall energy efficiency of the system.

[0054] The above-mentioned specific implementation can be partially adjusted in different ways by those skilled in the art without departing from the principle and purpose of the present invention. The protection scope of the present invention shall be based on the claims and shall not be limited by the above-mentioned specific implementation. Each implementation scheme within its scope shall be subject to the constraints of the present invention.

Claims

1. A cold-heat-electricity-fuel-oxygen cogeneration system, characterized in that: include: A carbon capture module, an energy storage module and a fuel preparation module, wherein: the carbon capture module captures carbon dioxide, absorbs heat from the heat storage tank during the desorption process and outputs the carbon dioxide to the energy storage module and the fuel preparation module respectively; the energy storage module compresses carbon dioxide during the charging process and stores the compression heat of the compression process, and outputs electrical energy to the fuel preparation module or the power grid during the discharging process; the fuel preparation module uses the heat of the electric heater and the electrolysis product to obtain high-temperature water vapor and high-temperature carbon dioxide, uses the electrical energy output by the energy storage module and the off-peak electricity for electrolysis, and outputs the heat energy to the carbon capture module and the energy storage module respectively; The carbon capture module comprises: a blower, a carbon dioxide adsorption unit, a carbon dioxide desorption unit and a vacuum pump connected in sequence; The energy storage module comprises: a first heat exchanger, a first condenser, a second heat exchanger, a low-pressure carbon dioxide storage tank, a throttle valve, a third heat exchanger, a carbon dioxide compression pressure regulating device, a second condenser, a high-pressure carbon dioxide storage tank, a centrifugal pump, a carbon dioxide expansion pressure regulating device, a heat exchange fluid unit, a heat storage tank, a cold exchange fluid unit and a cold storage tank connected in sequence; The fuel preparation module comprises: a high-temperature solid oxide electrolysis cell, a fourth heat exchanger, a fifth heat exchanger and a methanation reactor; The high-temperature solid oxide electrolytic cell comprises: an air blower, an air preheat exchanger, a first electric heater and an electrolytic cell anode connected in sequence, a carbon dioxide blower, a carbon dioxide preheat exchanger, a mixer, a second electric heater and an electrolytic cell cathode connected in sequence, and a water pump, a steam generator, and a steam preheat exchanger connected in sequence; The carbon capture module specifically comprises: a blower (1), a carbon dioxide adsorption unit (2), a carbon dioxide desorption unit (3) and a vacuum pump (4) connected in sequence, wherein: the input end of the carbon dioxide desorption unit (3) is respectively connected to the heat exchange fluid unit (16), the heat storage tank (17) and the vacuum pump (4) of the energy storage module, and the vacuum pump (4) is connected to the hot side inlet end of the first heat exchanger (5) of the energy storage module and the carbon dioxide blower (2004) of the high-temperature solid oxide electrolysis cell; The energy storage module specifically comprises: a first heat exchanger (5), a first condenser (6), a second heat exchanger (7), a low-pressure carbon dioxide storage tank (8), a throttle valve (9), a third heat exchanger (10), a carbon dioxide compression pressure regulating device (11), a second condenser (12), a high-pressure carbon dioxide storage tank (13), a centrifugal pump (14), a carbon dioxide expansion pressure regulating device (15), a heat exchange fluid unit (16), a heat storage tank (17), a cold exchange fluid unit (18) and a cold storage tank (19) which are connected in sequence, wherein: the hot side outlet end, the cold side inlet end and the cold side outlet end of the first heat exchanger (5) are respectively connected to the first condenser (6), the heat exchange fluid unit (16) and the heat storage tank (17); the hot side outlet end, the cold side inlet end and the cold side outlet end of the second heat exchanger (7) are respectively connected to the low-pressure carbon dioxide storage tank (8), the cold storage tank (19) and the cold exchange fluid unit (18); the cold side outlet end, the hot side inlet end and the cold side outlet end of the third heat exchanger (10) are respectively connected to the low-pressure carbon dioxide storage tank (8), the cold storage tank (19) and the cold exchange fluid unit (18); The inlet end and the hot side outlet end are respectively connected to the inlet end of the first stage compressor (1101A), the cold exchange fluid unit (18), and the cold storage tank (19); the outlet end of the valve (11V001) is connected to the second condenser (12); the outlet ends of the valves (11V1C), (11V2C), (11Vn-1C), and (11VnC) are connected to the carbon dioxide blower (2004) of the high temperature solid oxide electrolysis cell; the centrifugal pump (14) is connected to the first stage expansion unit (1101A); The cold side inlet of the expansion heat exchanger (1501A) is connected, the outlet of the valve (15V001) is connected to the hot side inlet of the first heat exchanger (5), the outlet of the valve (15V002) is connected to the hot side inlet of the second heat exchanger (7), and the outlets of the valves (15V1C), (15V2C), (15Vn-1C), (15VnC), and (15V003) are connected to the carbon dioxide blower (2004) of the high-temperature solid oxide electrolysis cell; The fuel preparation module specifically comprises: a high-temperature solid oxide electrolysis cell (20), a fourth heat exchanger (21), a fifth heat exchanger (22) and a methanation reactor (23), wherein: the high-temperature solid oxide electrolysis cell (20) is connected to a vacuum pump (4), a carbon dioxide compression pressure regulating device (11), a carbon dioxide expansion pressure regulating device (15), a fourth heat exchanger (21), and a fifth heat exchanger (22); the cold side inlet end and the cold side outlet end of the fourth heat exchanger (21) are respectively connected to a heat exchange fluid unit (16) and a heat storage tank (17); the hot side outlet end, the cold side inlet end, and the cold side outlet end of the fifth heat exchanger (22) are respectively connected to a methanation reactor (23), a heat exchange fluid unit (16), and a heat storage tank (17); and the methanation reactor (23) is connected to a heat exchange fluid unit (16) and a heat storage tank (17); The high temperature solid oxide electrolytic cell specifically comprises: an air blower (2001), an air preheat exchanger (2002), a first electric heater (2003) and an electrolytic cell anode (2011) connected in sequence, a carbon dioxide blower (2004), a carbon dioxide preheat exchanger (2005), a mixer (2009), a second electric heater (2010) and an electrolytic cell cathode (2013) connected in sequence, and a water pump (2006), a steam generator (2007) and a steam preheat exchanger (2008) connected in sequence, wherein: the air blower ( 2001) is connected to the ambient air and the cold side inlet of the air preheat exchanger (2002), the cold side outlet, hot side inlet and hot side outlet of the air preheat exchanger (2002) are respectively connected to the first electric heater (2003), the anode of the high temperature solid oxide electrolysis cell (2011) and the hot side inlet of the steam generator (2007), the first electric heater (2003) is connected to the anode of the high temperature solid oxide electrolysis cell (2011), the carbon dioxide blower (2004) is connected to the outlet of the carbon capture module vacuum pump (4), the energy storage module valve (11V1C), ( The outlet ends of (11V2C), (11Vn-1C), (11VnC), (15V1C), (15V2C), (15Vn-1C), (15VnC), and (15V003) are connected; the cold side inlet end, cold side outlet end, hot side inlet end, and hot side outlet end of the carbon dioxide preheat exchanger (2005) are connected to the carbon dioxide blower (2004), the mixer (2009), the cathode of the high temperature solid oxide electrolysis cell (2013), and the hot side inlet end of the steam preheat exchanger (2008), respectively; the water pump (2006) is connected to the ambient water and steam The cold side inlet end of the generator (2007) is connected, the cold side outlet end and the hot side inlet end of the steam generator (2007) are respectively connected to the steam preheat exchanger (2008) and the hot side outlet end of the air preheat exchanger (2002), the cold side outlet end and the hot side inlet end of the steam preheat exchanger (2008) are respectively connected to the mixer (2009) and the hot side outlet end of the carbon dioxide preheat exchanger (2005), the mixer (2009) is connected to the second electric heater (2010), and the second electric heater (2010) is connected to the cathode (2013) of the high-temperature solid oxide electrolysis cell.

2. The cold-heat-electricity-fuel-oxygen cogeneration system according to claim 1 is characterized in that: The carbon dioxide compression and pressure regulating device specifically comprises: a first-stage compressor (1101A), a first-stage pressure sensor (11P1), a valve (11V1), a first-stage compression heat exchanger (1101B), a valve (11V1B), a second-stage compressor (1102A), a second-stage pressure sensor (11P2), a valve (11V2), a second-stage compression heat exchanger (1102B), a valve (11V2B), an n-1th-stage compressor (11n-1A), an n-1th-stage pressure sensor (11Pn-1), and a valve (11Vn-1) connected in sequence. , n-1 stage compression heat exchanger (11n-1B), valve (11Vn-1B), n stage compressor (11nA), n stage pressure sensor (11Pn), valve (11Vn), n stage compression heat exchanger (11nB), valve (11VnA), valve (11V001) and valve (11V1A), valve (11V1C), valve (11V2A), valve (11V2C), valve (11Vn-1A), valve (11Vn-1C), valve (11VnC), wherein: first to n stage compression heat exchangers (1101B), (1102B), (11n-1B), (11nB ) the cold side inlet and the cold side outlet are respectively connected to the heat exchange fluid unit (16) and the heat storage tank (17); the inlet ends of valves (11V1A), (11V2A), and (11Vn-1A) are respectively connected to the hot side outlet ends of the first to n-1 stage compression heat exchangers (1101B), (1102B), and (11n-1B); the outlet ends are connected to the inlet end of valve (11V001); the inlet ends of valves (11V1C), (11V2C), (11Vn-1C), and (11Vn-1C) are respectively connected to the outlet ends of the first stage pressure sensors (11P1), (11P2), (11Pn-1), and (11Pn); The carbon dioxide compression and pressure regulating device is divided into the first to third layers from top to bottom, the first to nth stage compressors (1101A), (1102A), (11n-1A), (11nA), valves (11V1A), (11V2A), (11Vn-1A), (11VnA), (11V1B), (11V2B), (11Vn-1B), (11V001), the first inlet, and the first outlet are located on the first layer of the device, and the first to nth stage compression heat exchangers are located on the first layer of the device. Devices (1101B), (1102B), (11n-1B), (11nB), valves (11V1), (11V2), (11Vn-1), (11Vn), (11V1C), (11V2C), (11Vn-1C), (11VnC), first-stage pressure sensors (11P1), (11P2), (11Pn-1), (11Pn), the second inlet and the third outlet are located on the second layer of the device, and the second outlet is located on the third layer of the device.

3. The cold-heat-electricity-fuel-oxygen cogeneration system according to claim 1 is characterized in that: The carbon dioxide expansion pressure regulating device comprises: a first-stage expansion heat exchanger (1501A), a first-stage pressure sensor (15P1), a valve (15V1), a first-stage expansion machine (1501B), a valve (15V1B), a first-stage temperature sensor (15T1), a valve (15V1D), a first-stage cold storage heat exchanger (1501C), a valve (15V1F), a second-stage expansion heat exchanger (1502A), a second-stage pressure sensor (15P2), a valve (15V2), a second-stage expansion machine (1502B), a valve (15V2B), a second-stage temperature sensor (15T2), a valve (15V2D), a first-stage cold storage heat exchanger (1502C), a valve (1 5V2F), n-1 stage expansion heat exchanger (15n-1A), n-1 stage n-1 pressure sensor (15Pn-1), valve (15Vn-1), n-1 stage expansion machine (15n-1B), valve (15Vn-1B), n-1 stage temperature sensor (15Tn-1), valve (15Vn-1D), n-1 stage cold storage heat exchanger (15n-1C), valve (15Vn-1F), n-1 stage expansion heat exchanger (15nA), n-1 stage pressure sensor (15Pn), valve (15Vn), n-1 stage expansion machine (15nB), valve (15VnA), temperature sensor (15T001) and valve (15V1A), valve (15V1C), Valve (15V1E), valve (15V2A), valve (15V2C), valve (15V2E), valve (15Vn-1A), valve (15Vn-1C), valve (15Vn-1E), valve (15VnC), valve (15V001), valve (15V002), valve (15V003), wherein: the hot side inlet and hot side outlet of the first to nth stage expansion heat exchangers (1501A), (1502A), (15n-1A), (15nA) are respectively connected to the heat storage tank (17) and the heat exchange fluid unit (16), and the hot side inlet and hot side outlet of the first to n-1th stage cold storage heat exchangers (1501C), (1502C), (15n-1C) are respectively connected to the heat storage tank (17) and the heat exchange fluid unit (16). The inlet ends are respectively connected to the cold exchange fluid unit (18) and the cold storage tank (19); the inlet ends of the valves (15V1A), (15V2A), and (15Vn-1A) are respectively connected to the outlet ends of the first to n-1 stage expansion machines (1501B), (1502B), and (15n-1B); the outlet ends are connected to the inlet end of the temperature sensor (15T001); the inlet ends of the valves (15V1C), (15V2C), (15Vn-1C), and (15VnC) are respectively connected to the outlet ends of the first stage pressure sensors (15P1), (15P2), (15Pn-1), and (15Pn); the inlet end of the valve (15V001) is connected to the outlet end of the temperature sensor (15T001);The outlet end is connected to the inlet end of the hot side of the first heat exchanger (5), the inlet end of the valve (15V002) is connected to the outlet end of the temperature sensor (15T001), the outlet end is connected to the inlet end of the hot side of the second heat exchanger (7), and the inlet end of the valve (15V003) is connected to the outlet end of the valve (15VnA); The carbon dioxide expansion and pressure regulating device is divided into the first to fourth layers from top to bottom, the first to nth stage expansion machines (1501B), (1502B), (15n-1B), (15nB), valves (15V1A), (15V2A), (15Vn-1A), (15VnA), (15V1B), (15V2B), (15Vn-1B), (15V001), (15V002), (15V003), temperature sensor (15T001), the first outlet and the second outlet are located on the first layer of the device, the first to n-1th stage cold storage heat exchangers (1501C), (1502C), (15n-1C), valves (15V1D), (15V1E), (15V1F), (15V2D), (15V2E), (15V2F), (15Vn-1D), (15Vn-1E), (15Vn-1F), the first stage temperature sensor (15T1), (15T2), (15Tn-1), the third inlet and the fifth outlet are located on the second layer of the device, the first to nth stage expansion heat exchangers (1501A), (1502A), (15n-1A), (15nA), the first stage pressure sensor (15P1), (15P2), (15Pn-1), (15Pn), valves (15V1), (15V2), (15Vn-1), (15Vn), (15V1C), (15V2C), (15Vn-1C), (15VnC), the first inlet, the second inlet and the fourth outlet are located on the third layer of the device, and the third outlet is located on the fourth layer of the device.

4. A method for cogeneration of cold, heat, electricity, fuel and oxygen according to any one of claims 1 to 3, wherein the cold, heat, electricity, fuel and oxygen supply modes, the fuel and oxygen supply modes and the cold, heat, electricity, fuel and oxygen multi-energy cogeneration modes are respectively implemented according to the load demand of the power grid and the energy demand of the surrounding areas of the system; The said based on the grid load demand and the system's surrounding energy conditions means: when the grid load is low, the charging stage of the cold, heat and electricity supply mode and the cold, heat and electricity, fuel and oxygen multi-energy supply mode is carried out; when the grid load is high, the discharging stage of the cold, heat and electricity supply mode and the cold, heat and electricity, fuel and oxygen multi-energy supply mode is carried out; when the system's surrounding energy has a high demand for cold, heat and electricity and the provided cold, heat and electricity can meet the demand, the cold, heat and electricity supply mode is adopted; when the system's surrounding energy has a low demand for cold, heat and electricity, the fuel and oxygen supply mode is adopted; when the system's surrounding energy has a high demand for cold, heat and electricity and the provided cold, heat and electricity is far greater than the surrounding demand, the cold, heat and electricity, fuel and oxygen multi-energy supply mode is adopted.

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