CN113653548B - Multi-circulation coupling combined supply system with chemical quality improvement and heat storage functions - Google Patents
Multi-circulation coupling combined supply system with chemical quality improvement and heat storage functions Download PDFInfo
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
- F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
- F01K27/00—Plants for converting heat or fluid energy into mechanical energy, not otherwise provided for
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
- F01D—NON-POSITIVE DISPLACEMENT MACHINES OR ENGINES, e.g. STEAM TURBINES
- F01D15/00—Adaptations of machines or engines for special use; Combinations of engines with devices driven thereby
- F01D15/10—Adaptations for driving, or combinations with, electric generators
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
- F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
- F01K11/00—Plants characterised by the engines being structurally combined with boilers or condensers
- F01K11/02—Plants characterised by the engines being structurally combined with boilers or condensers the engines being turbines
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
- F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
- F01K25/00—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for
- F01K25/08—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for using special vapours
- F01K25/10—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for using special vapours the vapours being cold, e.g. ammonia, carbon dioxide, ether
- F01K25/103—Carbon dioxide
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D20/00—Heat storage plants or apparatus in general; Regenerative heat-exchange apparatus not covered by groups F28D17/00 or F28D19/00
- F28D20/003—Heat storage plants or apparatus in general; Regenerative heat-exchange apparatus not covered by groups F28D17/00 or F28D19/00 using thermochemical reactions
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
- Y02E60/14—Thermal energy storage
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Abstract
A multi-cycle coupling combined supply system with chemical quality improvement and heat storage, belonging to the technical field of energy storage; the system comprises three subsystems, namely a Rankine cycle subsystem, a carbon dioxide cycle subsystem and a chemical upgrading and heat storage subsystem; the system can realize the storage and quality improvement of low-grade heat energy, and utilizes the medium-grade heat energy and the high-grade heat energy after quality improvement to combine with carbon dioxide circulation and organic Rankine cycle to produce electric energy, thereby realizing cogeneration.
Description
Technical Field
The invention relates to a multi-cycle coupling combined supply system with chemical quality improvement and heat storage, and belongs to the technical field of energy storage.
Background
The energy consumption in the industrial field of China is about 70% of the total national energy consumption, and the unit energy consumption of main industrial products is about 30% higher than the international advanced level. Besides the factors of relatively backward production industry and unreasonable industrial structure, the low industrial waste heat utilization rate and the insufficient energy utilization are important reasons for high energy consumption, the energy utilization rate in China is only about 33 percent, and the energy consumption is about 10 percent lower than that in developed countries, and at least 50 percent of industrial energy consumption is directly abandoned in various forms of waste heat. Therefore, from another perspective, the industrial waste heat resource in China is abundant and widely exists in the production process of various industries, the waste heat resource accounts for about 17% -67% of the total energy consumption of the industrial waste heat, the recovery rate can reach 60%, the waste heat utilization rate is large in lifting space, and the energy saving potential is huge. If a proper heat storage scheme can be designed, the heat of the part of waste heat and waste heat is stored, and a proper mode is selected to utilize the stored heat for heat supply and power supply, so that the utilization rate of energy sources can be improved, and huge economic and environmental benefits can be brought. Therefore, it is important to select a suitable heat storage mode and to select a method for reasonably utilizing low-temperature heat energy.
As for the heat storage mode, there are sensible heat storage, latent heat storage and chemical heat storage in the heat storage field at present. Sensible heat storage and latent heat storage are widely applied, but the further application of the device is limited by the defects of non-constant temperature of sensible heat storage and heat release, small heat storage density, huge heat storage device and the like; the latent heat storage is phase change heat storage, is greatly influenced by the phase change temperature of the material and has great technical difficulty; and sensible heat storage and latent heat storage are limited by heat exchange temperature difference and heat exchanger area, so that the grade of heat energy is inevitably reduced in the heat storage process, and the heat energy is greatly lost in long-term storage, so that the heat storage efficiency is reduced. The chemical heat storage is to store heat energy in a chemical energy form by utilizing a pair of chemical reactions of positive and negative suction/heat release, the energy storage density is obviously higher than that of the sensible heat storage and the latent heat storage, and the reaction process can be controlled by a catalyst or a reactant, so that the long-term storage of the heat can be realized without almost loss, but the heat exchange process still exists in the chemical heat storage, the grade of the heat energy is still reduced, and the waste heat cannot be effectively utilized. For the heat energy stored in the heat storage system, the utilization modes of the heat energy are different according to the energy grade, and the high-grade heat energy can be used for waste heat power generation.
The effective waste heat power generation technology comprises carbon dioxide circulation, organic Rankine circulation, kalina circulation and the like; in different temperature ranges, the organic Rankine cycle system adopts different low-boiling-point organic working media to replace water, absorbs heat energy to generate electricity, has higher cycle heat efficiency, but has less net work output to the outside,
the efficiency is low; the carbon dioxide circulation takes carbon dioxide as a working medium of the power circulation, and the carbon dioxide circulation can output larger net work, but the return period and investment cost are larger, and the circulation thermal efficiency is lower; the single use of the organic Rankine cycle and the carbon dioxide cycle for power generation has certain drawbacks.
Disclosure of Invention
Aiming at the defects and defects of the prior art, the invention provides a multi-cycle coupling combined supply system based on chemical quality improvement and heat accumulation. The system comprises three subsystems, namely a Rankine cycle subsystem, a carbon dioxide cycle subsystem and a chemical upgrading and heat storage subsystem. The system can realize the storage and quality improvement of low-grade heat energy, and can realize the cogeneration by utilizing the medium-high grade heat energy after quality improvement and combining carbon dioxide circulation and organic Rankine cycle to produce electric energy.
The technical scheme of the invention is as follows:
A multi-cycle coupling combined supply system with chemical quality improvement and heat storage is characterized in that: the system is composed of an organic Rankine cycle subsystem, a carbon dioxide cycle subsystem and a chemical upgrading and heat accumulating subsystem. The chemical upgrading and heat storage subsystem is used for finishing the upgrading and storage functions of external low-grade heat energy, and is respectively connected with the organic Rankine cycle subsystem and the carbon dioxide cycle subsystem in series through pipelines, and the organic Rankine cycle subsystem and the carbon dioxide cycle subsystem are used for generating power by using the medium-high grade heat energy after the chemical upgrading and heat storage subsystem is upgraded in a grading manner.
A multi-cycle coupling combined supply system with chemical quality improvement and heat storage is characterized in that: the chemical upgrading and heat storage subsystem comprises a medium-low temperature waste heat storage unit, a chemical heat pump upgrading unit and a medium-high temperature heat storage unit; the medium-low temperature waste heat storage unit comprises a medium-low temperature waste heat chemical storage device, a medium-low temperature heat storage device, a medium-low temperature product storage tank, an endothermic reaction device and a gas compressor, wherein the medium-low temperature waste heat chemical storage device is internally filled with reaction raw materials based on a chemical heat storage principle, and the reaction raw materials can undergo forward endothermic reaction (the reverse reaction is exothermic reaction); the chemical heat pump upgrading unit comprises an endothermic reaction device, a rectifying tower, a separation device, a regenerator and a medium-high temperature heat energy chemical storage device, wherein the endothermic reaction device is internally filled with reaction raw materials based on a chemical heat storage principle, and the reaction raw materials can undergo forward endothermic reaction in a low-temperature environment (reverse reaction in a high-temperature environment, and the reverse reaction is exothermic reaction); the medium-high temperature heat storage unit comprises a medium-high temperature heat energy chemical storage device, a medium-high temperature heat storage device, a medium-high temperature product storage tank, a valve and a gas compressor, wherein the medium-high temperature heat energy chemical storage device is internally filled with reaction raw materials based on a chemical heat storage principle, and the reaction raw materials can undergo forward endothermic reaction (the reverse reaction is exothermic reaction).
The organic Rankine cycle subsystem comprises an organic working medium storage tank, an organic working medium pump, an organic working medium evaporator, an organic working medium turbine, a generator and an organic working medium condenser.
The carbon dioxide circulation subsystem comprises a carbon dioxide storage tank, a carbon dioxide pump, a carbon dioxide evaporator, a carbon dioxide turbine, a generator and a carbon dioxide condenser.
A multi-cycle coupling combined supply system with chemical quality improvement and heat storage is characterized by comprising the following equipment connection characteristics:
in the chemical upgrading and heat storage subsystem, an outlet of an internal heat exchanger of a medium-low temperature waste heat chemical storage device of a medium-low temperature waste heat storage unit is connected with a heat source inlet of the medium-low temperature heat storage device through a pipeline; the reaction product outlet of the medium-low temperature waste heat chemical storage device is connected with the inlet of the medium-low temperature product storage tank through a pipeline through an internal heat exchanger of the heat absorption reaction device, the medium-low temperature heat storage device and the air compressor; and an outlet of the medium-low temperature product storage tank is connected with a reaction product inlet of the medium-low temperature waste heat chemical storage device through a pipeline and a valve by the medium-low temperature heat storage device.
In the chemical upgrading and heat storage subsystem, a reaction raw material-reaction product outlet of an endothermic reaction device of a chemical heat pump upgrading unit is connected with a reaction raw material-reaction product inlet of a separation device through a pipeline by a reaction raw material-reaction product channel of a rectifying tower; the reaction product outlet of the separation device is connected with the inlet of the internal reactor pipeline of the medium-temperature thermal energy chemical storage device through a reaction product channel of the heat regenerator by a pipeline; the outlet of the pipeline of the internal reactor of the medium-temperature high-temperature thermal energy chemical storage device is connected with the reaction raw material inlet of the endothermic reaction device through a reaction raw material channel of the heat regenerator by a pipeline; the reaction raw material outlet of the separation device is connected with the reaction raw material inlet of the rectifying tower through a pipeline; and the reaction raw material outlet of the rectifying tower is connected with the reaction raw material inlet of the endothermic reaction device through a pipeline.
In the chemical upgrading and heat storage subsystem, a reaction product outlet of a medium-high temperature heat energy chemical storage device of a medium-high temperature heat storage unit is connected with an inlet of a medium-high temperature product storage tank through a reaction product channel, a gas compressor and a valve of the medium-high temperature heat storage device by pipelines; and an outlet of the medium-high temperature product storage tank is connected with a reaction product inlet of the medium-high temperature heat energy chemical storage device through a reaction product channel of the medium-high temperature heat storage device by a pipeline.
In the organic Rankine cycle subsystem, the organic working medium storage tank is connected with an organic working medium pump through a pipeline; the organic working medium pump is connected with the organic working medium evaporator through a pipeline; the organic working medium evaporator is connected with the organic working medium turbine through a pipeline; the organic working medium turbine is connected with the organic working medium condenser through a pipeline; the organic working medium condenser is connected with the organic working medium storage tank through a pipeline; the rotating shaft of the organic working medium turbine is connected with the input shaft of the generator.
In the carbon dioxide circulation subsystem, the carbon dioxide storage tank is connected with a carbon dioxide pump through a pipeline; the carbon dioxide pump is connected with the carbon dioxide evaporator through a pipeline; the carbon dioxide evaporator is connected with a carbon dioxide turbine through a pipeline; the carbon dioxide turbine is connected with the carbon dioxide condenser through a pipeline; the carbon dioxide condenser is connected with the carbon dioxide storage tank through a pipeline; the rotating shaft of the carbon dioxide turbine is connected with the input shaft of the generator.
A multi-cycle coupling combined supply system with chemical quality improvement and heat storage is characterized by comprising the following steps:
firstly, a waste heat-carrying medium with a certain temperature enters an internal heat exchanger of a medium-low temperature waste heat chemical storage device of a chemical upgrading and heat storage subsystem to exchange heat with the medium-low temperature heat storage device, and is discharged to the external environment after the temperature is reduced.
And then, the chemical upgrading and heat accumulating subsystem starts to work, and the working process is divided into two stages of energy storage and energy release. In the energy storage stage, in the medium-low temperature waste heat storage unit, the reaction raw materials stored in the medium-low temperature waste heat chemical storage device absorb heat from a waste heat carrying medium through an internal heat exchanger, the reaction raw materials absorb heat and raise temperature, a forward endothermic reaction occurs at a proper temperature and pressure, and the reaction products contain solid, gaseous or liquid products; separating the products according to the different phases and densities of the products, and leaving the solid products with high density in the medium-low temperature waste heat chemical storage device; the gaseous or liquid product with a certain temperature and small density enters an internal heat exchanger of the endothermic reaction device to exchange heat under the action of the air compressor, the temperature of the gaseous or liquid product with a certain temperature and small density after heat exchange is reduced and enters the medium-low temperature heat storage device to further release heat, and then the gaseous or liquid product is sent into the medium-low temperature product storage tank for storage through the air compressor, so that the medium-low temperature waste heat storage process is completed.
In the energy storage stage, the reaction raw materials in the heat absorption reaction device absorb heat from gaseous or liquid products with certain temperature and small density through an internal heat exchanger, the reaction raw materials absorb heat and raise temperature, forward endothermic reaction occurs at proper temperature and pressure, and the reaction products and part of unreacted reaction raw materials are conveyed to a rectifying tower; in the rectifying tower, according to the difference of boiling points of the reaction product and the reaction raw material, the reaction product and the reaction raw material are separated, most of the reaction raw material with higher boiling point is remained in the rectifying tower and is then discharged back to the endothermic reaction device, and the reaction product with certain temperature and lower boiling point and a small amount of reaction raw material are discharged out of the rectifying tower and enter a separation device; in the separation device, the reaction raw material and the reaction product are further separated to obtain a high-purity reaction product, the separated reaction raw material is sent back to the rectifying tower, and the high-purity reaction product enters the heat regenerator; in the regenerator, the high-purity reaction product absorbs heat and rises in temperature and then enters an internal reactor pipeline of the medium-temperature high-temperature thermal energy chemical storage device; in the internal reactor pipeline of the middle-high temperature thermal energy chemical storage device, the high-purity reaction product is subjected to reverse exothermic reaction at proper temperature and pressure, the released heat is absorbed by the reaction raw material filled outside the internal reactor pipeline of the middle-high temperature thermal energy chemical storage device, and meanwhile, the reaction raw material with a certain temperature and unreacted reaction product generated by the reverse exothermic reaction are conveyed to a regenerator; in the regenerator, the reaction raw materials with a certain temperature and unreacted reaction products exchange heat with the high-purity reaction products from the separation device, and after the heat exchange is finished, the temperature of the reaction raw materials with a certain temperature and the unreacted reaction products is reduced and conveyed to the endothermic reaction device, so that the low-temperature waste heat upgrading process is finished.
In the energy storage stage, the reaction raw materials filled outside the internal reactor pipeline of the medium-high temperature thermal energy chemical storage device absorb heat and then heat up, a forward endothermic reaction occurs at a proper temperature and pressure, the reaction products contain solid, gaseous or liquid products, then the products are separated according to the different phases and densities of the products, the solid products with high density are left in the medium-high temperature thermal energy chemical storage device, and the gaseous or liquid products with certain temperature and low density are discharged out of the medium-high temperature thermal energy chemical storage device under the suction action of the gas compressor; the gaseous or liquid product with a certain temperature and small density is subjected to heat exchange through the medium-high temperature heat storage device, heat is stored in the medium-high temperature heat storage device, after the heat exchange is finished, the temperature of the gaseous or liquid product with a certain temperature and small density is reduced, and the gaseous or liquid product is sent into the medium-high temperature product storage tank through the air compressor to be stored, so that the medium-high temperature heat energy storage process is finished.
In the energy release stage, in the medium-low temperature waste heat storage unit, a gaseous or liquid product in a medium-low temperature product storage tank enters a medium-low temperature heat storage device for heat exchange, is preheated to a certain temperature and then enters a medium-low temperature waste heat chemical storage device, and is subjected to reverse exothermic reaction with an original solid product in the medium-low temperature waste heat chemical storage device at a proper temperature and pressure, and the released heat passes through an internal heat exchanger in the medium-low temperature waste heat chemical storage device to heat domestic water; meanwhile, in the medium-high temperature heat storage unit, gaseous or liquid products in the medium-high temperature product storage tank are discharged, heat exchange is carried out through the medium-high temperature heat storage device, the products are preheated to a certain temperature and then enter the medium-high temperature heat energy chemical storage device, and reverse exothermic reaction is carried out between the products and the original solid products in the medium-high temperature heat energy chemical storage device at proper temperature and pressure.
When electricity is used up to a peak, the carbon dioxide circulation subsystem and the organic Rankine cycle subsystem start to work, heat exchange oil absorbs heat released by chemical reaction through an internal heat exchanger of the medium-temperature high-temperature thermal energy chemical storage device, and the heat exchange oil with the temperature increased sequentially passes through an organic working medium evaporator and a carbon dioxide evaporator to heat organic working medium and carbon dioxide. The organic working medium absorbs heat to become superheated steam, the superheated steam expands in an organic working medium turbine to do work, and the organic working medium turbine rotates to drive a generator to generate electricity; the carbon dioxide absorbs heat and becomes a supercritical state, the carbon dioxide expands in a carbon dioxide turbine to do work, and the carbon dioxide turbine rotates to drive a generator to generate electricity.
The invention has the following advantages and outstanding technical effects:
1. the chemical upgrading and heat storage subsystem combines chemical heat storage with chemical upgrading based on the chemical upgrading and heat storage principle, sequentially stores low-temperature heat energy, chemically upgrades and stores medium-high temperature heat, improves the grade of low-temperature waste heat while storing heat, has high heat storage density, small heat loss, high heat storage efficiency and good economic benefit, and expands the application range of heat energy.
2. The organic Rankine cycle subsystem and the carbon dioxide cycle subsystem of the invention utilize the medium-high grade heat energy after the chemical upgrading and heat storage subsystem is upgraded in a grading way to generate power. Compared with directly utilizing waste heat, waste heat is used as a heat source of a subsystem, medium and high grade heat energy is used as an evaporation heat source, and the evaporation temperature of working media is improved, so that the circulation efficiency, the net work amount and the economy are improved; compared with the single use of the organic Rankine cycle or the carbon dioxide cycle, the two cycles are simultaneously coupled, so that the heat efficiency is improved, the generated energy is also improved, and the method has good economic benefit.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings that are needed in the embodiments are briefly described below, and it is obvious that the drawings in the following description are only some embodiments of the present invention and that other drawings can be obtained according to these drawings without inventive effort for a person skilled in the art.
FIG. 1 shows a multi-cycle coupling combined supply system with chemical quality improvement and heat storage.
The list of the reference numerals in the drawings is: 1-a carbon dioxide storage tank; 2-carbon dioxide pump; 3-carbon dioxide evaporator; 4-carbon dioxide turbine; a 5-carbon dioxide condenser; 6-an organic working medium storage tank; 7-an organic working fluid pump; 8-an organic working medium evaporator; 9-an organic working medium turbine; 10-an organic working medium condenser; 11-a medium-low temperature heat storage device; 12-a medium-low temperature product storage tank; 13-a medium-low temperature waste heat chemical storage device; 14-an endothermic reaction device; 15-a rectifying tower; 16-separation means; 17-a regenerator; 18-medium-high temperature thermal energy chemical storage device; 19-a medium-high temperature heat storage device; 20-a medium-high temperature product storage tank; 21 22-valve; 23-a heat exchange oil pump; 24 A 25-generator; i, II, III, IV-internal heat exchangers; a, B-compressor.
Detailed Description
The principles and embodiments of the present invention are further described below with reference to the drawings.
A multi-cycle coupling combined supply system with chemical quality improvement and heat storage is characterized in that: the system comprises three subsystems, namely a mechanical Rankine cycle subsystem, a carbon dioxide cycle subsystem and a chemical upgrading and heat storage subsystem. The chemical upgrading and heat storage subsystem is used for finishing the upgrading and storage functions of external low-grade heat energy, and is respectively connected with the organic Rankine cycle subsystem and the carbon dioxide cycle subsystem in series through pipelines, and the organic Rankine cycle subsystem and the carbon dioxide cycle subsystem are used for generating power by using the medium-high grade heat energy after the chemical upgrading and heat storage subsystem is upgraded in a grading manner.
The chemical upgrading and heat storage subsystem comprises a medium-low temperature waste heat storage unit, a chemical heat pump upgrading unit and a medium-high temperature heat storage unit.
The medium-low temperature waste heat storage unit of the chemical upgrading and heat storage subsystem comprises a medium-low temperature heat storage device 11, a medium-low temperature product storage tank 12, a medium-low temperature waste heat chemical storage device 13, a heat absorption reaction device 14, a gas compressor B and a valve 22; the medium-low temperature waste heat chemical storage device 13 is internally filled with a reaction raw material based on a chemical heat storage principle, and the reaction raw material can undergo a forward endothermic reaction (the reverse reaction is an exothermic reaction); the chemical heat pump upgrading unit of the chemical upgrading and heat accumulating subsystem comprises a heat absorption reaction device 14, a rectifying tower 15, a separation device 16, a heat regenerator 17 and a medium-temperature thermal energy chemical storage device 18, wherein the heat absorption reaction device 14 is internally filled with reaction raw materials based on a chemical heat accumulation principle, and the reaction raw materials can undergo forward heat absorption reaction in a low-temperature environment (undergo reverse reaction in a high-temperature environment, and the reverse reaction is exothermic reaction); the medium-high temperature heat storage unit of the chemical upgrading heat storage subsystem comprises a medium-high temperature heat storage device 18, a medium-high temperature heat storage device 19, a medium-high temperature product storage tank 20, a valve 21 and a gas compressor A, wherein the medium-high temperature heat storage device 18 is internally filled with reaction raw materials based on a chemical heat storage principle, and the reaction raw materials can undergo a forward endothermic reaction (the reverse reaction is an exothermic reaction).
The organic Rankine cycle subsystem comprises an organic working medium storage tank 6, an organic working medium pump 7, an organic working medium evaporator 8, an organic working medium turbine 9, an organic working medium condenser 10 and a generator 25.
The carbon dioxide circulation subsystem comprises a carbon dioxide storage tank 1, a carbon dioxide pump 2, a carbon dioxide evaporator 3, a carbon dioxide turbine 4, a carbon dioxide condenser 5 and a generator 24.
A multi-cycle coupling combined supply system with chemical quality improvement and heat storage is characterized by comprising the following equipment connection characteristics:
in the chemical upgrading and heat storage subsystem, an outlet of an internal heat exchanger I of a medium-low temperature waste heat chemical storage device 13 of a medium-low temperature waste heat storage unit is connected with a waste heat medium heat source inlet 11d of a medium-low temperature heat storage device 11 through a pipeline; the reaction product outlet of the medium-low temperature waste heat chemical storage device 13 is connected with the inlet of the internal heat exchanger III of the endothermic reaction device 14 through a pipeline; the outlet of the internal heat exchanger III of the endothermic reaction device 14 is connected with a reaction product heat source inlet 11a of the medium-low temperature heat storage device 11 through a pipeline; the reaction product outlet 11B of the medium-low temperature heat storage device 11 is connected with the inlet of the air compressor B through a pipeline; the outlet of the compressor B is connected with the inlet of the medium-low temperature product storage tank 12 through a pipeline; the outlet of the medium-low temperature product storage tank 12 is connected with a reaction product cold source inlet 11e of the medium-low temperature heat storage device 11 through a pipeline and a valve 22; the reaction product cold source outlet 11f of the medium-low temperature heat storage device 11 is connected with the reaction product inlet of the medium-low temperature waste heat chemical storage device 13 through a pipeline.
In the chemical upgrading and heat storage subsystem, a reaction raw material-reaction product outlet 14a of an endothermic reaction device 14 of a chemical heat pump upgrading unit is connected with a reaction raw material-reaction product inlet 15a of a rectifying tower 15 through a pipeline; the reaction raw material outlet 15d of the rectifying tower 15 is connected with the reaction raw material inlet 14c of the endothermic reaction device 14 through a pipeline, and the reaction raw material-reaction product outlet 15b of the rectifying tower 15 is connected with the reaction raw material-reaction product inlet 16a of the separation device 16 through a pipeline; the reaction product outlet 16b of the separation device 16 is connected with the reaction product inlet 17a of the regenerator 17 through a pipeline, and the reaction raw material outlet 16c of the separation device 16 is connected with the reaction raw material inlet 15c of the rectifying tower 15 through a pipeline; the reaction raw material outlet 17d of the heat regenerator 17 is connected with the reaction raw material inlet 14b of the endothermic reaction device 14 through a pipeline, and the reaction product outlet 17b of the heat regenerator 17 is connected with the internal reactor pipeline inlet 18a of the medium-temperature thermal energy chemical storage device 18 through a pipeline; the internal reactor pipe outlet 18b of the medium-temperature thermal energy chemical storage device 18 is connected with the reaction raw material inlet 17c of the regenerator 17 through a pipe.
In the chemical upgrading and heat storage subsystem, a reaction product outlet 18d of a medium-high temperature heat energy chemical storage device 18 of the medium-high temperature heat storage unit is connected with a heat source inlet 19c of a medium-high temperature heat storage device 19 through a pipeline; the heat source outlet 19d of the medium-high temperature heat storage device 19 is connected with the inlet of the air compressor A through a pipeline; the outlet of the compressor A is connected with the inlet of the medium-high temperature product storage tank 20 through a pipeline and a valve 21; the outlet of the medium-high temperature product storage tank 20 is connected with a cold source inlet 19b of the medium-high temperature heat storage device 19 through a pipeline; the cold source outlet 19a of the medium-high temperature heat storage device 19 is connected with the reaction product inlet 18c of the medium-high temperature heat chemical storage device 18 through a pipeline.
In the carbon dioxide circulation subsystem, an outlet 1b of a carbon dioxide pump storage tank 1 is connected with an inlet 2a of a carbon dioxide pump 2 through a pipeline; the outlet 2b of the carbon dioxide pump 2 is connected with the cold source side inlet of the carbon dioxide evaporator 3 through a pipeline; the outlet of the cold source side of the carbon dioxide evaporator 3 is connected with an inlet 4a of a carbon dioxide turbine 4 through a pipeline; the outlet 4b of the carbon dioxide turbine 4 is connected with the inlet 5a of the carbon dioxide condenser 5 through a pipeline; the outlet 5b of the carbon dioxide condenser 5 is connected with the inlet 1a of the carbon dioxide storage tank 1 through a pipeline; the rotary shaft of the carbon dioxide turbine 4 is connected to the input shaft of the generator 24.
In the organic Rankine cycle subsystem, an outlet 6b of an organic working medium storage tank 6 is connected with an inlet 7a of an organic working medium pump 7 through a pipeline; the outlet 7b of the organic working medium pump 7 is connected with the cold source side inlet of the organic working medium evaporator 8 through a pipeline; the outlet of the cold source side of the organic working medium evaporator 8 is connected with an inlet 9a of the organic working medium turbine 9 through a pipeline; the outlet 9b of the organic working medium turbine 9 is connected with the inlet 10a of the organic working medium condenser 10 through a pipeline; the outlet 10b of the organic working medium condenser 10 is connected with the inlet 6a of the organic working medium storage tank 6 through a pipeline; the rotating shaft of the organic working medium turbine 9 is connected to the input shaft of the generator 25.
An outlet 23b of the heat exchange oil pump 23 is connected with an inlet of an internal heat exchanger IV of the medium-temperature heat energy chemical storage device 18 through a pipeline; the outlet of the internal heat exchanger IV of the medium-temperature heat energy chemical storage device 18 is connected with the heat source inlet of the organic working medium evaporator 8 through a pipeline; the heat source outlet of the organic working medium evaporator 8 is connected with the heat source inlet of the carbon dioxide evaporator 3 through a pipeline; the outlet of the heat source of the carbon dioxide evaporator 3 is connected with the inlet 23a of the working medium pump 23 through a pipeline.
A multi-cycle coupling combined supply system with chemical quality improvement and heat storage is characterized by comprising the following steps:
firstly, 110-120 ℃ waste heat carrying medium (such as water, flue gas and the like) enters an internal heat exchanger I of a medium-low temperature waste heat chemical storage device 13 for heat exchange, the temperature of the waste heat carrying medium after heat exchange is reduced, the waste heat carrying medium enters a medium-low temperature heat storage device 11 for further heat release, and then the waste heat is discharged to the external environment.
Then, the chemical upgrading and heat accumulating subsystem works, and the working process is divided into two stages of energy storage and energy release. In the energy storage stage, the medium-low temperature waste heat is converted into heat in the medium-low temperature waste heat storage unitChemical heat storage medium (hydrogen storage alloy NaAlH) stored inside the chemical storage device 13 4 ) The hydrogen storage alloy NaAlH absorbs heat from the waste heat carrying medium through the internal heat exchanger I 4 The forward endothermic decomposition reaction occurs at 105 ℃, and the reaction formula is:
the reaction generates hydrogen with the temperature of about 105 ℃, then the hydrogen enters an internal heat exchanger III of the endothermic reaction device 14 for heat exchange under the action of a gas compressor B, the temperature of the hydrogen is reduced after the heat exchange and the hydrogen enters a medium-low temperature heat storage device 11 for further heat release, and then the hydrogen is sent into a medium-low temperature product storage tank 12 for storage through the gas compressor B, so that the medium-low temperature waste heat storage process is completed.
In the energy storage stage, in the chemical heat pump upgrading unit, a chemical heat storage medium (liquid isopropanol) in the endothermic reaction device 14 absorbs heat from hydrogen through internal heat exchange III, the liquid isopropanol absorbs heat and heats up to evaporate, then a forward endothermic decomposition reaction occurs at about 90 ℃, the catalyst is a ZnO/CuO composite catalyst, and the reaction formula is as follows:
(CH 3 ) 2 CHOH(l)→(CH 3 ) 2 CHOH(g) ΔH＝45.4kJ/mol
(CH 3 ) 2 CHOH(g)→(CH 3 ) 2 CO(g)+H 2 (g) ΔH＝55.0kJ/mol
the reaction generates acetone and hydrogen with the temperature of about 90 ℃, and then, mixed gas of the acetone and the hydrogen with the temperature of about 90 ℃ and part of unreacted gaseous isopropanol enter a rectifying tower 15; in the rectifying tower 15, according to the difference of the boiling points of the mixed gas of acetone and hydrogen and gaseous isopropanol, most of the gaseous isopropanol is condensed and liquefied so as to be separated from the mixed gas of acetone and hydrogen, the liquid isopropanol obtained by condensation and liquefaction is then discharged back to the endothermic reaction device 14, the mixed gas of hydrogen and acetone at about 80 ℃ and a small amount of gaseous isopropanol which is not condensed and liquefied are discharged out of the rectifying tower 15 and enter the separating device 16; in the separation device 16, the residual gaseous isopropanol is separated and returned to the rectifying tower 15, and meanwhile, high-purity acetone and hydrogen mixed gas at about 80 ℃ is obtained, and then the high-purity acetone and hydrogen mixed gas at about 80 ℃ enters the heat regenerator 17; in the heat regenerator 17, the mixed gas of high-purity acetone and hydrogen at about 80 ℃ absorbs heat, and the temperature rises to about 200 ℃ and then enters an internal reactor pipeline of the medium-temperature thermal energy chemical storage device 18; the internal reactor pipeline of the medium-temperature high-temperature thermal energy chemical storage device 18 is filled with a solid catalyst Raney Ni, and the mixed gas of high-purity acetone and hydrogen at about 200 ℃ is catalyzed by the solid catalyst Raney Ni to undergo a reverse exothermic chemical combination reaction to generate gaseous isopropanol at about 250 ℃, wherein the reaction formula is as follows:
(CH 3 ) 2 CO(g)+H 2 (g)→(CH 3 ) 2 CHOH(g) ΔH＝-55.0kJ/mol
The heat released by the reaction is externally filled by the internal reactor tube of the medium-temperature thermal energy chemical storage device 18 with the reaction raw material hydrogen storage alloy Mg 2 NiH 4 Absorbing, and then discharging the gaseous isopropyl alcohol at about 250 ℃ and the mixed gas of unreacted hydrogen and acetone back to the heat regenerator 17; in the regenerator 17, the gaseous isopropyl alcohol at about 250 ℃ and the unreacted hydrogen and acetone exchange heat with the mixed gas of high-purity acetone and hydrogen at about 80 ℃ from the separation device 16, and after the heat exchange is completed, the temperature of the gaseous isopropyl alcohol at about 250 ℃ and the mixed gas of unreacted hydrogen and acetone is reduced to about 80 ℃ and is returned to the endothermic reaction device 14, thereby completing the low-temperature waste heat upgrading process.
In the energy storage stage, the medium-high temperature heat storage unit is filled with reactant Mg outside the internal reactor tube of the medium-high temperature thermal energy chemical storage device 18 2 NiH 4 After absorbing heat, gradually heating, and carrying out forward endothermic decomposition reaction at about 240 ℃, wherein the reaction formula is as follows:
Mg 2 NiH 4 (s)→Mg 2 Ni(s)+2H 2 (g) ΔH＝65kJ/mol
the reaction generates hydrogen with the temperature of about 240 ℃, and then the hydrogen with the temperature of about 240 ℃ is discharged out of the medium-temperature thermal energy chemical storage device 18 under the suction action of the air compressor A and enters the medium-temperature thermal energy storage device 19; the hydrogen with the temperature of about 240 ℃ exchanges heat through the medium-high temperature heat storage device 19, the heat of the hydrogen with the temperature of about 240 ℃ is stored in the medium-high temperature heat storage device 19, the temperature of the hydrogen with the temperature of about 240 ℃ is reduced after the heat exchange is completed, and then the hydrogen is sent into the medium-high temperature product storage tank 20 for storage through the gas compressor A, so that the medium-high temperature heat energy storage process is completed.
In the energy release stage, in the medium-low temperature waste heat storage unit, the hydrogen in the medium-low temperature product storage tank 12 enters the medium-low temperature heat storage device 11 to exchange heat, and after the heat exchange, the hydrogen is preheated to about 95 ℃ and enters the medium-low temperature waste heat chemical storage device 13 to be mixed with the original solid product Na at the temperature of 90 DEG C 3 AlH 6 Al undergoes reverse chemical combination exothermic reaction, and the reaction formula is as follows:
the released heat is used for heating domestic water through an internal heat exchanger II of the medium-low temperature waste heat chemical storage device 13, so that the heat supply process is completed; in the medium-high temperature heat storage unit, hydrogen in the medium-high temperature product storage tank 20 enters the medium-high temperature heat storage device 19 to exchange heat, after the heat exchange is finished, the hydrogen is preheated to about 220 ℃ and enters the medium-high temperature heat energy chemical storage device 18, and the hydrogen and the original solid product Mg in the medium-high temperature heat energy chemical storage device at about 220 DEG C 2 Ni undergoes reverse chemical combination exothermic reaction, and the reaction formula is:
Mg 2 Ni(s)+2H 2 (g)→Mg 2 NiH 4 (s) ΔH＝-65kJ/mol
the released heat heats the heat exchange oil through the heat exchanger IV of the medium-temperature thermal energy chemical storage device 18; when electricity is used up to peak, the heat exchange oil absorbing heat sequentially passes through the organic working medium evaporator 8, the carbon dioxide evaporator 3 and heats n-pentane and carbon dioxide; meanwhile, n-pentane in the organic working medium storage tank 6 enters the organic working medium pump 7 and is compressed to a set working pressure of 1.9Mpa, the pressurized n-pentane is sent to the organic working medium evaporator 8 to absorb heat, the n-pentane is changed into superheated steam after absorbing heat, the superheated steam enters the organic working medium turbine 9 to expand and do work, the organic working medium turbine 9 rotates to drive the generator 25 to generate power, the n-pentane after doing work is discharged out of the organic working medium turbine 9 and enters the organic working medium condenser 10, the condensing pressure is 0.1Mpa, the condensing temperature is 35 ℃, and the liquid n-pentane is continuously absorbed by the organic working medium evaporator 8 after being pressurized, and the medium-high grade heat energy after being upgraded by the chemical upgrading heat storage subsystem; carbon dioxide in the carbon dioxide storage tank 1 enters the carbon dioxide pump 2 and is compressed to a set working pressure of 13Mpa, the pressurized carbon dioxide is sent to the carbon dioxide evaporator 3 to absorb heat and is changed into a supercritical state, the supercritical carbon dioxide enters the carbon dioxide turbine 4 to expand and do work, the carbon dioxide turbine 4 rotates to drive the generator 24 to generate power, the carbon dioxide after doing work is discharged out of the carbon dioxide turbine 4 and enters the carbon dioxide condenser 5 to be condensed, and the condensed carbon dioxide is pressurized and then enters the carbon dioxide evaporator 3 to continuously absorb medium-high grade heat energy after quality improvement of the chemical quality improvement heat storage subsystem, so that the power supply process is completed.
In the embodiment, the medium-high grade heat energy after being upgraded by the chemical upgrading and heat accumulating subsystem can be coupled with other circulating power generation modes, such as: the kalina cycle, the brayton cycle, the stirling cycle, etc., are not limited to the organic rankine cycle and the carbon dioxide cycle described above.
Finally, the above examples are only intended to aid in understanding the method of the invention and its core ideas; also, as will occur to those of ordinary skill in the art, variations in the specific embodiments and in the scope of the applications based on the teachings herein. In view of the foregoing, the description of the present invention should not be construed as limiting the invention.
Claims (2)
1. A multi-cycle coupling combined supply system with chemical quality improvement and heat storage is characterized in that: the system comprises three subsystems, namely an organic Rankine cycle subsystem, a carbon dioxide cycle subsystem and a chemical upgrading and heat storage subsystem; the chemical upgrading and heat storage subsystem is used for finishing the upgrading and storage functions of external low-grade heat energy, and is respectively connected with the organic Rankine cycle subsystem and the carbon dioxide cycle subsystem in series through pipelines, and the organic Rankine cycle subsystem and the carbon dioxide cycle subsystem are used for generating power by using the medium-high grade heat energy after the chemical upgrading and heat storage subsystem is upgraded in a grading manner;
The medium-low temperature waste heat storage unit of the chemical upgrading and heat storage subsystem comprises a medium-low temperature heat storage device (11), a medium-low temperature product storage tank (12), a medium-low temperature waste heat chemical storage device (13), an endothermic reaction device (14), a gas compressor B and a valve II (22), wherein the medium-low temperature waste heat chemical storage device (13) is internally filled with a reaction raw material based on a chemical heat storage principle, the reaction raw material can undergo a forward endothermic reaction, and the reverse reaction is an exothermic reaction; the chemical heat pump upgrading unit of the chemical upgrading and heat accumulating subsystem comprises an endothermic reaction device (14), a rectifying tower (15), a separation device (16), a heat regenerator (17) and a medium-high temperature heat energy chemical storage device (18), wherein the endothermic reaction device (14) is internally filled with reaction raw materials based on a chemical heat accumulation principle, the reaction raw materials can undergo forward endothermic reaction in a low-temperature environment and undergo reverse reaction in a high-temperature environment, and the reverse reaction is exothermic reaction; the medium-high temperature heat storage unit of the chemical upgrading heat storage subsystem comprises a medium-high temperature heat storage device (18), a medium-high temperature heat storage device (19), a medium-high temperature product storage tank (20), a first valve (21) and a gas compressor A, wherein the medium-high temperature heat storage device (18) is internally filled with reaction raw materials based on a chemical heat storage principle, the reaction raw materials can undergo a forward endothermic reaction, and a reverse reaction is an exothermic reaction;
The organic Rankine cycle subsystem comprises an organic working medium storage tank (6), an organic working medium pump (7), an organic working medium evaporator (8), an organic working medium turbine (9), an organic working medium condenser (10) and a second generator (25);
the carbon dioxide circulation subsystem comprises a carbon dioxide storage tank (1), a carbon dioxide pump (2), a carbon dioxide evaporator (3), a carbon dioxide turbine (4), a carbon dioxide condenser (5) and a first generator (24);
in the chemical upgrading and heat storage subsystem, an outlet of an internal heat exchanger I of a medium-low temperature waste heat chemical storage device (13) of a medium-low temperature waste heat storage unit is connected with a waste heat medium-carrying heat source inlet (11 d) of a medium-low temperature heat storage device (11) through a pipeline; the reaction product outlet of the medium-low temperature waste heat chemical storage device (13) is connected with the inlet of an internal heat exchanger III of the endothermic reaction device (14) through a pipeline; the outlet of the internal heat exchanger III of the endothermic reaction device (14) is connected with a reaction product heat source inlet (11 a) of the medium-low temperature heat storage device (11) through a pipeline; the reaction product outlet (11B) of the medium-low temperature heat storage device (11) is connected with the inlet of the air compressor B through a pipeline; the outlet of the air compressor B is connected with the inlet of the medium-low temperature product storage tank (12) through a pipeline; the outlet of the medium-low temperature product storage tank (12) is connected with a reaction product cold source inlet (11 e) of the medium-low temperature heat storage device (11) through a pipeline and a valve II (22); the reaction product cold source outlet (11 f) of the medium-low temperature heat storage device (11) is connected with the reaction product inlet of the medium-low temperature waste heat chemical storage device (13) through a pipeline;
In the chemical upgrading and heat storage subsystem, a reaction raw material-reaction product outlet (14 a) of an endothermic reaction device (14) of a chemical heat pump upgrading unit is connected with a reaction raw material-reaction product inlet (15 a) of a rectifying tower (15) through a pipeline; the reaction raw material outlet (15 d) of the rectifying tower (15) is connected with the reaction raw material inlet (14 c) of the endothermic reaction device (14) through a pipeline, and the reaction raw material-reaction product outlet (15 b) of the rectifying tower (15) is connected with the reaction raw material-reaction product inlet (16 a) of the separation device (16) through a pipeline; the reaction product outlet (16 b) of the separation device (16) is connected with the reaction product inlet (17 a) of the heat regenerator (17) through a pipeline, and the reaction raw material outlet (16 c) of the separation device (16) is connected with the reaction raw material inlet (15 c) of the rectifying tower (15) through a pipeline; the reaction raw material outlet (17 d) of the heat regenerator (17) is connected with the reaction raw material inlet (14 b) of the endothermic reaction device (14) through a pipeline, and the reaction product outlet (17 b) of the heat regenerator (17) is connected with the internal reactor pipeline inlet (18 a) of the medium-high-temperature thermal energy chemical storage device (18) through a pipeline; an internal reactor pipeline outlet (18 b) of the medium-temperature thermal energy chemical storage device (18) is connected with a reaction raw material inlet (17 c) of the regenerator (17) through a pipeline;
In the carbon dioxide circulation subsystem, an outlet (1 b) of a carbon dioxide storage tank (1) is connected with an inlet (2 a) of a carbon dioxide pump (2) through a pipeline; an outlet (2 b) of the carbon dioxide pump (2) is connected with a cold source side inlet of the carbon dioxide evaporator (3) through a pipeline; the cold source side outlet of the carbon dioxide evaporator (3) is connected with an inlet (4 a) of the carbon dioxide turbine (4) through a pipeline; an outlet (4 b) of the carbon dioxide turbine (4) is connected with an inlet (5 a) of the carbon dioxide condenser (5) through a pipeline; an outlet (5 b) of the carbon dioxide condenser (5) is connected with an inlet (1 a) of the carbon dioxide pump storage tank (1) through a pipeline; the rotating shaft of the carbon dioxide turbine (4) is connected with the input shaft of the first generator (24);
in the organic Rankine cycle subsystem, an outlet (6 b) of an organic working medium storage tank (6) is connected with an inlet (7 a) of an organic working medium pump (7) through a pipeline; an outlet (7 b) of the organic working medium pump (7) is connected with a cold source side inlet of the organic working medium evaporator (8) through a pipeline; the outlet of the cold source side of the organic working medium evaporator (8) is connected with an inlet (9 a) of the organic working medium turbine (9) through a pipeline; an outlet (9 b) of the organic working medium turbine (9) is connected with an inlet (10 a) of the organic working medium condenser (10) through a pipeline; an outlet (10 b) of the organic working medium condenser (10) is connected with an inlet (6 a) of the organic working medium storage tank (6) through a pipeline; the rotating shaft of the organic working medium turbine (9) is connected with the input shaft of the generator II (25);
An outlet (23 b) of the heat exchange oil pump (23) is connected with an inlet of an internal heat exchanger IV of the medium-temperature heat energy chemical storage device (18) through a pipeline; the outlet of the internal heat exchanger IV of the medium-temperature heat energy chemical storage device (18) is connected with the heat source inlet of the organic working medium evaporator (8) through a pipeline; the heat source outlet of the organic working medium evaporator (8) is connected with the heat source inlet of the carbon dioxide evaporator (3) through a pipeline; the heat source outlet of the carbon dioxide evaporator (3) is connected with the inlet (23 a) of the heat exchange oil pump (23) through a pipeline.
2. The multi-cycle coupling and co-supplying system with chemical upgrading and heat storage according to claim 1, wherein the system is characterized by comprising the following steps:
firstly, a waste heat-carrying medium with a certain temperature enters an internal heat exchanger I of a medium-low temperature waste heat chemical storage device (13) of a chemical upgrading and heat storage subsystem to exchange heat with a medium-low temperature heat storage device (11), and after the temperature is reduced, the medium is discharged to the external environment;
then, the chemical upgrading and heat accumulating subsystem starts to work, and the working process is divided into two stages of energy storage and energy release; in the energy storage stage, in the medium-low temperature waste heat storage unit, the reaction raw materials stored in the medium-low temperature waste heat chemical storage device (13) absorb heat from a waste heat carrying medium through an internal heat exchanger I, the reaction raw materials absorb heat and raise temperature, a forward endothermic reaction occurs at a proper temperature and pressure, and the reaction products contain solid, gaseous or liquid products; separating the products according to the different phases and densities of the products, and leaving the solid products with high density in a medium-low temperature waste heat chemical storage device (13); the gaseous or liquid product with certain temperature and small density enters an internal heat exchanger III of the heat absorption reaction device (14) for heat exchange, the temperature of the gaseous or liquid product with certain temperature and small density after heat exchange is reduced and enters a medium-low temperature heat storage device (11) for further heat release, and then the gaseous or liquid product is sent into a medium-low temperature product storage tank (12) for storage through a gas compressor B, so that the medium-low temperature waste heat storage process is completed;
In the energy storage stage, in the chemical heat pump upgrading unit, the reaction raw materials in the endothermic reaction device (14) absorb heat from gaseous or liquid products with certain temperature and small density through an internal heat exchanger III, the reaction raw materials absorb heat and raise temperature, forward endothermic reaction occurs at proper temperature and pressure, and the reaction products and part of unreacted reaction raw materials are conveyed to the rectifying tower (15); in the rectifying tower (15), according to the difference of boiling points of reaction products and reaction raw materials, the reaction products and the reaction raw materials are separated, most of the reaction raw materials with higher boiling points are left in the rectifying tower (15) and then are discharged back to the endothermic reaction device (14), and the reaction products with certain temperature and lower boiling points and a small amount of reaction raw materials are discharged out of the rectifying tower (15) and enter the separating device (16); in the separation device (16), the reaction raw material and the reaction product are further separated to obtain a high-purity reaction product, the separated reaction raw material is sent back to the rectifying tower (15), and the high-purity reaction product enters the heat regenerator (17); in the regenerator (17), the high purity reaction product absorbs heat and warms up and then enters the internal reactor tube of the medium-temperature thermal energy chemical storage device (18); in the internal reactor pipeline of the middle-high temperature thermal energy chemical storage device (18), the high-purity reaction product is subjected to inverse exothermic reaction at proper temperature and pressure, the released heat is absorbed by the reaction raw material filled outside the internal reactor pipeline of the middle-high temperature thermal energy chemical storage device (18), and meanwhile, the reaction raw material with a certain temperature and unreacted reaction product generated by the inverse exothermic reaction are conveyed to a regenerator (17); in the heat regenerator (17), the reaction raw materials with a certain temperature and unreacted reaction products exchange heat with the high-purity reaction products from the separation device (16), after the heat exchange is finished, the temperature of the reaction raw materials with a certain temperature and the unreacted reaction products is reduced and are conveyed to the endothermic reaction device (14), and the high-purity reaction products from the separation device (16) enter an internal reactor pipeline of the medium-temperature thermal energy chemical storage device (18) after absorbing heat and raising temperature, so that the low-temperature waste heat upgrading process is finished;
In the energy storage stage, the reaction raw materials filled outside the internal reactor pipeline of the medium-high temperature thermal energy chemical storage device (18) absorb heat and then heat up, a forward endothermic reaction occurs at a proper temperature and pressure, the reaction product contains solid, gaseous or liquid products, then the products are separated according to the different phases and densities of the products, the solid products with high density are left in the medium-high temperature thermal energy chemical storage device (18), and the gaseous or liquid products with certain temperature and low density are discharged out of the medium-high temperature thermal energy chemical storage device (18); the gaseous or liquid product with a certain temperature and small density exchanges heat through the medium-high temperature heat storage device (19), heat is stored in the medium-high temperature heat storage device (19), after the heat exchange is finished, the temperature of the gaseous or liquid product with a certain temperature and small density is reduced, and the gaseous or liquid product is sent into the medium-high temperature product storage tank (20) for storage through the air compressor A, so that the medium-high temperature heat energy storage process is finished;
in the energy release stage, in the medium-low temperature waste heat storage unit, a gaseous or liquid product in a medium-low temperature product storage tank (12) enters a medium-low temperature heat storage device (11) to exchange heat, and enters a medium-low temperature waste heat chemical storage device (13) after being preheated to a certain temperature, and the product and the original solid product in the medium-low temperature waste heat chemical storage device (13) undergo a reverse exothermic reaction at a proper temperature and pressure, and the released heat passes through an internal heat exchanger II in the medium-low temperature waste heat chemical storage device (13) to heat domestic water; meanwhile, in the medium-high temperature heat storage unit, gaseous or liquid products in the medium-high temperature product storage tank (20) are discharged, heat exchange is carried out through the medium-high temperature heat storage device (19), the products enter the medium-high temperature heat energy chemical storage device (18) after being preheated to a certain temperature, and the products and the solid products in the medium-high temperature heat energy chemical storage device (18) are subjected to reverse exothermic reaction at proper temperature and pressure;
When electricity consumption is high, the carbon dioxide circulation subsystem and the organic Rankine cycle subsystem start to work, heat exchange oil absorbs heat released by chemical reaction through an internal heat exchanger IV of a medium-temperature high-temperature heat energy chemical storage device (18), and the heat exchange oil with the temperature increased sequentially passes through an organic working medium evaporator (8) and a carbon dioxide evaporator (3) to heat organic working medium and carbon dioxide; the organic working medium in the organic working medium storage tank (6) enters the organic working medium pump (7) and is compressed to a set working pressure, the pressurized organic working medium is sent to the organic working medium evaporator (8) to absorb heat, the organic working medium absorbs heat and becomes superheated steam, the superheated steam expands in the organic working medium turbine (9) to do work, the organic working medium turbine (9) rotates to drive the generator II (25) to generate power, the organic working medium after doing work is discharged out of the organic working medium turbine (9) and enters the organic working medium condenser (10), and the liquid organic working medium is pressurized and then enters the organic working medium evaporator (8) to continuously absorb medium and high grade heat energy after the chemical working medium heat storage subsystem is upgraded; carbon dioxide in the carbon dioxide storage tank (1) enters the carbon dioxide pump (2) and is compressed to a set working pressure, the pressurized carbon dioxide is sent to the carbon dioxide evaporator (3) to absorb heat and becomes a supercritical state, the carbon dioxide expands and works in the carbon dioxide turbine (4), the carbon dioxide turbine (4) rotates to drive the generator I (24) to generate electricity, the carbon dioxide after working is discharged out of the carbon dioxide turbine (4) and enters the carbon dioxide condenser (5) to be condensed, and the carbon dioxide after condensation is pressurized and then enters the carbon dioxide evaporator (3) to continuously absorb medium-high grade heat energy after quality improvement of the chemical quality improvement heat storage subsystem so as to complete the power supply process.
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Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH11117713A (en) * | 1997-10-09 | 1999-04-27 | Hitachi Ltd | Chemical heat-accumulating type intake air cooling device |
| CN102817657A (en) * | 2012-09-12 | 2012-12-12 | 重庆大学 | Heat pipe technology based organic Rankine cycle low-temperature exhaust heat power generating system |
| CN105156163A (en) * | 2015-07-08 | 2015-12-16 | 清华大学 | Waste-heat utilization organic Rankine cycle system for fluctuant heat source |
| CN107514837A (en) * | 2017-09-04 | 2017-12-26 | 中国科学院工程热物理研究所 | The cooling heating and power generation system that heat pump couples with supercritical carbon dioxide Brayton cycle |
| CN109269129A (en) * | 2018-08-28 | 2019-01-25 | 南京工业大学 | Calcium circulation step thermochemical energy storage method and system |
| CN111799819A (en) * | 2019-08-30 | 2020-10-20 | 华北电力大学（保定） | Coal gasification solid oxide fuel cell hybrid energy storage power generation system |
-
2021
- 2021-07-24 CN CN202110860663.0A patent/CN113653548B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH11117713A (en) * | 1997-10-09 | 1999-04-27 | Hitachi Ltd | Chemical heat-accumulating type intake air cooling device |
| CN102817657A (en) * | 2012-09-12 | 2012-12-12 | 重庆大学 | Heat pipe technology based organic Rankine cycle low-temperature exhaust heat power generating system |
| CN105156163A (en) * | 2015-07-08 | 2015-12-16 | 清华大学 | Waste-heat utilization organic Rankine cycle system for fluctuant heat source |
| CN107514837A (en) * | 2017-09-04 | 2017-12-26 | 中国科学院工程热物理研究所 | The cooling heating and power generation system that heat pump couples with supercritical carbon dioxide Brayton cycle |
| CN109269129A (en) * | 2018-08-28 | 2019-01-25 | 南京工业大学 | Calcium circulation step thermochemical energy storage method and system |
| CN111799819A (en) * | 2019-08-30 | 2020-10-20 | 华北电力大学（保定） | Coal gasification solid oxide fuel cell hybrid energy storage power generation system |
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