CN113653548B - Multi-circulation coupling combined supply system with chemical quality improvement and heat storage functions - Google Patents

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

A multi-cycle coupled power supply system with chemical quality improvement and heat storage

Technical Field

The invention relates to a multi-cycle coupling system with chemical quality improvement and heat storage, belonging to the technical field of energy storage.

Background Art

Energy consumption in my country's industrial sector accounts for about 70% of the country's total energy consumption, and the unit energy consumption of major industrial products is about 30% higher than the international advanced level. In addition to the relatively backward production industry and unreasonable industrial structure, the low utilization rate of industrial waste heat and the lack of full utilization of energy are important reasons for the high energy consumption. my country's energy utilization rate is only about 33%, which is about 10% lower than that of developed countries. At least 50% of industrial energy consumption is directly abandoned in various forms of waste heat. Therefore, from another perspective, my country's industrial waste heat resources are rich and widely exist in the production process of various industries. Waste heat resources account for about 17%-67% of its total fuel consumption, of which the recyclable rate is 60%. There is a large room for improvement in waste heat utilization and huge energy-saving potential. If a suitable heat storage scheme can be designed to store the heat of this part of waste heat and waste heat, and choose a suitable way to use the stored heat for heating and power supply, it can not only improve the utilization rate of energy, but also bring huge economic and environmental benefits. Therefore, it is crucial to choose a suitable heat storage method and a method to reasonably utilize low-temperature thermal energy.

As for the heat storage methods, currently in the field of heat storage, there are sensible heat storage, latent heat storage and chemical heat storage. Sensible heat storage and latent heat storage are widely used, but the shortcomings of sensible heat storage such as non-constant temperature, low heat storage density and large heat storage device limit its further application; latent heat storage is phase change heat storage, which is greatly affected by the phase change temperature of the material and has high technical difficulty; and sensible heat storage and latent heat storage are limited by the heat exchange temperature difference and the area of the heat exchanger, and the heat energy quality is inevitably reduced during the heat storage process, and the loss of heat energy is large during long-term storage, resulting in a decrease in heat storage efficiency. Chemical heat storage uses a pair of positive and reverse absorption/release chemical reactions to store heat energy in the form of chemical energy. The energy storage density is significantly greater than sensible heat storage and latent heat storage, and the reaction process can be controlled by catalysts or reactants, which can achieve long-term heat storage with almost no loss, but chemical heat storage still has a heat exchange process, which will still cause a decrease in heat energy quality, and cannot achieve efficient utilization of waste heat and residual heat. For the thermal energy stored in the heat storage system, its utilization method will vary depending on its energy grade. High-grade thermal energy can be used for waste heat power generation.

效率较低；二氧化碳循环将二氧化碳作为动力循环的工质，二氧化碳循环可以输出较大的净功，但回本周期和投资费用较大，循环热效率较低；单一的利用有机朗肯循环和二氧化碳循环进行发电，都有一定的缺陷。Effective waste heat power generation technologies include carbon dioxide cycle, organic Rankine cycle, Kalina cycle, etc. In different temperature ranges, the organic Rankine cycle system uses different low-boiling point organic working fluids instead of water to absorb heat energy for power generation. The cycle thermal efficiency is high, but the net work output to the outside is small.

The efficiency is low; the carbon dioxide cycle uses carbon dioxide as the working fluid of the power cycle. The carbon dioxide cycle can output a large net work, but the payback period and investment cost are large, and the cycle thermal efficiency is low; the single use of organic Rankine cycle and carbon dioxide cycle for power generation has certain defects.

Summary of the invention

In view of the shortcomings and defects of the prior art, the present invention proposes a multi-cycle coupled supply system based on chemical upgrading and heat storage. The system described in the present invention includes three subsystems, namely, a mechanical Rankine cycle subsystem, a carbon dioxide cycle subsystem, and a chemical upgrading and heat storage subsystem. The system described in the present invention can realize the storage and upgrading of low-grade thermal energy, and utilize the upgraded medium- and high-grade thermal energy in combination with the carbon dioxide cycle and the organic Rankine cycle to produce electricity, thereby realizing cogeneration of heat and power.

The technical solution of the present invention is as follows:

A multi-cycle coupling and supply system with chemical upgrading and heat storage, characterized in that the system is composed of 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 completes the upgrading and storage functions of external low-grade thermal energy, and the chemical upgrading and heat storage subsystem is connected in series with the organic Rankine cycle subsystem and the carbon dioxide cycle subsystem through pipelines, and the organic Rankine cycle subsystem and the carbon dioxide cycle subsystem hierarchically utilize the medium and high-grade thermal energy upgraded by the chemical upgrading and heat storage subsystem to generate electricity.

A multi-cycle coupled supply system with chemical upgrading and heat storage, characterized in that: the chemical upgrading and heat storage subsystem includes three parts: a medium-low temperature waste heat storage unit, a chemical heat pump upgrading unit and a medium-high temperature heat storage unit; wherein, the medium-low temperature waste heat storage unit includes 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 compressor; the medium-low temperature waste heat chemical storage device is filled with reaction raw materials based on the chemical heat storage principle, and the reaction raw materials can undergo a forward endothermic reaction (the reverse reaction is an exothermic reaction); the chemical heat pump upgrading unit includes an endothermic reaction device, A distillation tower, a separation device, a heat regenerator and a medium-high temperature thermal energy chemical storage device, wherein the endothermic reaction device is filled with reaction raw materials based on the principle of chemical heat storage, and the reaction raw materials can undergo a forward endothermic reaction in a low-temperature environment (a reverse reaction occurs in a high-temperature environment, and the reverse reaction is an exothermic reaction); the medium-high temperature heat storage unit includes a medium-high temperature thermal energy chemical storage device, a medium-high temperature heat storage device, a medium-high temperature product storage tank, a valve and a compressor, wherein the medium-high temperature thermal energy chemical storage device is filled with reaction raw materials based on the principle of chemical heat storage, and the reaction raw materials can undergo a forward endothermic reaction (the reverse reaction is an exothermic reaction).

The organic Rankine cycle subsystem includes an organic working fluid storage tank, an organic working fluid pump, an organic working fluid evaporator, an organic working fluid turbine, a generator, and an organic working fluid condenser.

The carbon dioxide circulation subsystem includes 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 coupled power supply system with chemical quality improvement and heat storage, the equipment connection characteristics are as follows:

In the chemical upgrading and heat storage subsystem, the outlet of the internal heat exchanger of the medium-low temperature waste heat chemical storage device of the medium-low temperature waste heat storage unit is connected to the 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 to the inlet of the medium-low temperature product storage tank through a pipeline via the internal heat exchanger of the endothermic reaction device, the medium-low temperature heat storage device and the compressor; the outlet of the medium-low temperature product storage tank is connected to the reaction product inlet of the medium-low temperature waste heat chemical storage device through a pipeline and a valve via the medium-low temperature heat storage device.

In the chemical upgrading and heat storage subsystem, the reaction raw material-reaction product outlet of the endothermic reaction device of the chemical heat pump upgrading unit is connected to the reaction raw material-reaction product inlet of the separation device through a pipeline via the reaction raw material-reaction product channel of the distillation tower; the reaction product outlet of the separation device is connected to the internal reactor pipeline inlet of the medium- and high-temperature thermal energy chemical storage device through a pipeline via the reaction product channel of the regenerator; the internal reactor pipeline outlet of the medium- and high-temperature thermal energy chemical storage device is connected to the reaction raw material inlet of the endothermic reaction device through a pipeline via the reaction raw material channel of the regenerator; the reaction raw material outlet of the separation device is connected to the reaction raw material inlet of the distillation tower through a pipeline; the reaction raw material outlet of the distillation tower is connected to the reaction raw material inlet of the endothermic reaction device through a pipeline.

In the chemical upgrading heat storage subsystem, the reaction product outlet of the medium-high temperature thermal energy chemical storage device of the medium-high temperature thermal storage unit is connected to the inlet of the medium-high temperature product storage tank through a pipeline via the reaction product channel of the medium-high temperature thermal storage device, a compressor, and a valve; the outlet of the medium-high temperature product storage tank is connected to the reaction product inlet of the medium-high temperature thermal energy chemical storage device through a pipeline via the reaction product channel of the medium-high temperature thermal storage device.

In the organic Rankine cycle subsystem, the organic working fluid storage tank is connected to the organic working fluid pump through a pipeline; the organic working fluid pump is connected to the organic working fluid evaporator through a pipeline; the organic working fluid evaporator is connected to the organic working fluid turbine through a pipeline; the organic working fluid turbine is connected to the organic working fluid condenser through a pipeline; the organic working fluid condenser is connected to the organic working fluid storage tank through a pipeline; the rotating shaft of the organic working fluid turbine is connected to the input shaft of the generator.

In the carbon dioxide circulation subsystem, the carbon dioxide storage tank is connected to the carbon dioxide pump through a pipeline; the carbon dioxide pump is connected to the carbon dioxide evaporator through a pipeline; the carbon dioxide evaporator is connected to the carbon dioxide turbine through a pipeline; the carbon dioxide turbine is connected to the carbon dioxide condenser through a pipeline; the carbon dioxide condenser is connected to the carbon dioxide storage tank through a pipeline; the rotating shaft of the carbon dioxide turbine is connected to the input shaft of the generator.

A multi-cycle coupled power supply system with chemical quality improvement and heat storage, characterized in that the system is operated in the following steps:

First, the waste heat medium with a certain temperature enters the internal heat exchanger and the medium and low temperature heat storage device of the chemical upgrading and heat storage subsystem for heat exchange. After the temperature is reduced, it is discharged to the external environment.

Subsequently, the chemical quality improvement and heat storage subsystem starts to work, and the working process is divided into two stages: energy storage and energy release. In the energy storage stage, in the medium-low temperature waste heat storage unit, the reaction raw materials stored inside the medium-low temperature waste heat chemical storage device absorb heat from the waste heat medium through the internal heat exchanger, and the reaction raw materials absorb heat and heat up, and a positive endothermic reaction occurs at a suitable temperature and pressure, and the reaction products contain solid, gaseous or liquid products; then, according to the different phases and densities of the products, the products are separated, and the solid products with high density are left in the medium-low temperature waste heat chemical storage device; the gaseous or liquid products with a certain temperature and low density enter the internal heat exchanger of the endothermic reaction device for heat exchange under the action of the compressor, and after the heat exchange, the temperature of the gaseous or liquid products with a certain temperature and low density decreases and enters the medium-low temperature heat storage device to further release heat, and then is sent to the medium-low temperature product storage tank through the compressor for storage, thereby completing the medium-low temperature waste heat storage process.

In the energy storage stage, in the chemical heat pump upgrading unit, the reaction raw materials inside the endothermic reaction device absorb heat from the gaseous or liquid products with a certain temperature and low density through the internal heat exchanger, the reaction raw materials absorb heat and heat up, and a forward endothermic reaction occurs at a suitable temperature and pressure, and the reaction products and part of the unreacted reaction raw materials are transported to the distillation tower; in the distillation tower, the reaction products are separated from the reaction raw materials according to the difference in boiling points between the reaction products and the reaction raw materials, most of the reaction raw materials with higher boiling points remain in the distillation tower, and are then discharged back to the endothermic reaction device, and the reaction products with a certain temperature and lower boiling point and a small amount of reaction raw materials are discharged from the distillation tower and enter the separation device; in the separation device, the reaction raw materials and the reaction products are further separated to obtain high-purity reaction products, and the separated reaction raw materials are returned to the distillation tower, and the high-purity reaction products are The product enters the regenerator; in the regenerator, the high-purity reaction product absorbs heat and rises in temperature, and then enters the internal reactor pipe of the medium-high temperature thermal energy chemical storage device; in the internal reactor pipe of the medium-high temperature thermal energy chemical storage device, the high-purity reaction product undergoes a reverse exothermic reaction at a suitable temperature and pressure, and the released heat is absorbed by the reaction raw materials filled outside the internal reactor pipe of the medium-high temperature thermal energy chemical storage device, and at the same time, the reaction raw materials with a certain temperature and the unreacted reaction products generated by the reverse exothermic reaction are transported to the regenerator; in the regenerator, the reaction raw materials with a certain temperature and the unreacted reaction products exchange heat with the high-purity reaction products from the separation device. After the heat exchange is completed, the temperature of the reaction raw materials with a certain temperature and the unreacted reaction products decreases and is transported to the endothermic reaction device, thereby completing the low-temperature waste heat quality improvement process.

During the energy storage stage, in the medium and high temperature heat storage unit, the reaction raw materials filled outside the internal reactor pipe of the medium and high temperature thermal energy chemical storage device absorb heat and then heat up, and a forward endothermic reaction occurs at a suitable temperature and pressure. The reaction products include solid, gaseous or liquid products. Subsequently, the products are separated according to the different phases and densities of the products. The solid products with high density remain in the medium and high temperature thermal energy chemical storage device, and the gaseous or liquid products with a certain temperature and low density are discharged from the medium and high temperature thermal energy chemical storage device under the suction action of the compressor; the gaseous or liquid products with a certain temperature and low density are subjected to heat exchange through the medium and high temperature heat storage device, and the heat is stored in the medium and high temperature heat storage device. After the heat exchange is completed, the temperature of the gaseous or liquid products with a certain temperature and low density is reduced, and they are sent to the medium and high temperature product storage tank for storage through the compressor, thereby completing the medium and high temperature thermal energy storage process.

In the energy release stage, in the medium and low temperature waste heat storage unit, the gaseous or liquid product in the medium and low temperature product storage tank enters the medium and low temperature heat storage device for heat exchange, and enters the medium and low temperature waste heat chemical storage device after being preheated to a certain temperature, and undergoes a reverse exothermic reaction with the original solid product in the medium and low temperature waste heat chemical storage device at a suitable temperature and pressure, and the released heat heats domestic water through the internal heat exchanger in the medium and low temperature waste heat chemical storage device; at the same time, in the medium and high temperature heat storage unit, the gaseous or liquid product in the medium and high temperature product storage tank is discharged, and undergoes heat exchange through the medium and high temperature heat storage device, and enters the medium and high temperature thermal energy chemical storage device after being preheated to a certain temperature, and undergoes a reverse exothermic reaction with the original solid product in the medium and high temperature thermal energy chemical storage device at a suitable temperature and pressure.

During peak hours of electricity consumption, the carbon dioxide circulation subsystem and the organic Rankine cycle subsystem start to work, and the heat exchange oil absorbs the heat released by the chemical reaction through the internal heat exchanger of the medium-high temperature thermal energy chemical storage device. The heat exchange oil with increased temperature passes through the organic working fluid evaporator and the carbon dioxide evaporator in turn to heat the organic working fluid and carbon dioxide. The organic working fluid absorbs heat and becomes superheated steam, which expands and does work in the organic working fluid turbine, and the organic working fluid turbine rotates to drive the generator to generate electricity; carbon dioxide absorbs heat and becomes a supercritical state, and carbon dioxide expands and does work in the carbon dioxide turbine, and the carbon dioxide turbine rotates to drive the generator to generate electricity.

The present invention has the following advantages and outstanding technical effects:

1. The chemical upgrading heat storage subsystem described in the present invention is based on the chemical upgrading heat storage principle, combining chemical heat storage with chemical upgrading. The subsystem sequentially performs low-temperature thermal energy storage, chemical upgrading and medium- and high-temperature heat storage, and improves the quality of low-temperature waste heat while storing heat. The system has high heat storage density, small heat loss, high heat storage efficiency, and good economic benefits, which expands the application scope of thermal energy.

2. The organic Rankine cycle subsystem and the carbon dioxide cycle subsystem described in the present invention use the medium and high-grade thermal energy upgraded by the chemical upgrading and heat storage subsystem to generate electricity in a graded manner. Compared with the direct use of waste heat, the waste heat is used as the heat source of the subsystem, and the medium and high-grade thermal energy is used as the evaporation heat source, which increases the evaporation temperature of the working fluid, thereby improving the cycle efficiency, net work and economy; compared with the single use of the organic Rankine cycle or the carbon dioxide cycle, the simultaneous coupling of the two cycles not only improves the thermal efficiency, but also increases the power generation, and has good economic benefits.

BRIEF DESCRIPTION OF THE DRAWINGS

In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings required for use in the embodiments are briefly introduced below. Obviously, the drawings described below are only some embodiments of the present invention. For ordinary technicians in this field, other drawings can be obtained based on these drawings without paying creative work.

FIG1 is a multi-cycle coupled power supply system with chemical upgrading and heat storage provided by the present invention.

The list of reference numerals in the figure is: 1-carbon dioxide storage tank; 2-carbon dioxide pump; 3-carbon dioxide evaporator; 4-carbon dioxide turbine; 5-carbon dioxide condenser; 6-organic working fluid storage tank; 7-organic working fluid pump; 8-organic working fluid evaporator; 9-organic working fluid turbine; 10-organic working fluid condenser; 11-medium and low temperature heat storage device; 12-medium and low temperature product storage tank; 13-medium and low temperature waste heat chemical storage device; 14-endothermic reaction device; 15-distillation tower; 16-separation device; 17-regenerator; 18-medium and high temperature thermal energy chemical storage device; 19-medium and high temperature heat storage device; 20-medium and high temperature product storage tank; 21, 22-valve; 23-heat exchange oil pump; 24, 25-generator; I, II, III, IV-internal heat exchanger; A, B-compressor.

DETAILED DESCRIPTION

The principle and specific implementation modes of the present invention are further described below in conjunction with the accompanying drawings.

A multi-cycle coupling system with chemical upgrading and heat storage, characterized in that the system includes 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 completes the upgrading and storage functions of external low-grade thermal energy, and the chemical upgrading and heat storage subsystem is connected in series with the organic Rankine cycle subsystem and the carbon dioxide cycle subsystem through pipelines, and the organic Rankine cycle subsystem and the carbon dioxide cycle subsystem hierarchically utilize the medium and high-grade thermal energy upgraded by the chemical upgrading and heat storage subsystem to generate electricity.

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 and low temperature waste heat storage unit of the chemical upgrading and heat storage subsystem includes a medium and low temperature heat storage device 11, a medium and low temperature product storage tank 12, a medium and low temperature waste heat chemical storage device 13, an endothermic reaction device 14, a compressor B, and a valve 22; the medium and low temperature waste heat chemical storage device 13 is filled with reaction raw materials based on the chemical heat storage principle, and the reaction raw materials 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 storage subsystem includes an endothermic reaction device 14, a distillation tower 15, a separation device 16, a regenerator 17 and a medium and high temperature thermal energy chemical storage device 18. The interior of the endothermic reaction device 14 is filled with reaction raw materials based on the principle of chemical heat storage, and the reaction raw materials can undergo a forward endothermic reaction in a low-temperature environment (a reverse reaction occurs in a high-temperature environment, and the reverse reaction is an exothermic reaction); the medium- and high-temperature heat storage unit of the chemical quality improvement heat storage subsystem includes a medium- and high-temperature thermal energy chemical storage device 18, a medium- and high-temperature heat storage device 19, a medium- and high-temperature product storage tank 20, a valve 21 and a compressor A. The interior of the medium- and high-temperature thermal energy chemical storage device 18 is filled with reaction raw materials based on the principle of chemical heat storage, and the reaction raw materials can undergo a forward endothermic reaction (the reverse reaction is an exothermic reaction).

The organic Rankine cycle subsystem includes an organic working fluid storage tank 6 , an organic working fluid pump 7 , an organic working fluid evaporator 8 , an organic working fluid turbine 9 , an organic working fluid condenser 10 , and a generator 25 .

The carbon dioxide circulation subsystem includes 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 coupled power supply system with chemical quality improvement and heat storage, the equipment connection characteristics are as follows:

In the chemical quality improvement heat storage subsystem, the outlet of the internal heat exchanger I of the medium-low temperature waste heat chemical storage device 13 of the medium-low temperature waste heat storage unit is connected to the heat source inlet 11d of the waste heat medium of the 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 to 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 to the 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 to the inlet of the compressor B through a pipeline; the outlet of the compressor B is connected to 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 to the 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 to 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, the reaction raw material-reaction product outlet 14a of the endothermic reaction device 14 of the chemical heat pump upgrading unit is connected to the reaction raw material-reaction product inlet 15a of the distillation tower 15 through a pipeline; the reaction raw material outlet 15d of the distillation tower 15 is connected to 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 distillation tower 15 is connected to 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 to the regenerator 1 through a pipeline. 7, the reaction product inlet 17a of the separation device 16 is connected to the reaction raw material inlet 15c of the distillation tower 15 through a pipeline; the reaction raw material outlet 17d of the regenerator 17 is connected to the reaction raw material inlet 14b of the endothermic reaction device 14 through a pipeline, and the reaction product outlet 17b of the regenerator 17 is connected to the internal reactor pipeline inlet 18a of the medium- and high-temperature thermal energy chemical storage device 18 through a pipeline; the internal reactor pipeline outlet 18b of the medium- and high-temperature thermal energy chemical storage device 18 is connected to the reaction raw material inlet 17c of the regenerator 17 through a pipeline.

In the chemical upgrading heat storage subsystem, the reaction product outlet 18d of the medium-high temperature thermal energy chemical storage device 18 of the medium-high temperature thermal storage unit is connected to the heat source inlet 19c of the medium-high temperature thermal storage device 19 through a pipeline; the heat source outlet 19d of the medium-high temperature thermal storage device 19 is connected to the inlet of the compressor A through a pipeline; the outlet of the compressor A is connected to 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 to the cold source inlet 19b of the medium-high temperature thermal storage device 19 through a pipeline; the cold source outlet 19a of the medium-high temperature thermal storage device 19 is connected to the reaction product inlet 18c of the medium-high temperature thermal energy chemical storage device 18 through a pipeline.

In the carbon dioxide circulation subsystem, the outlet 1b of the carbon dioxide pump storage tank 1 is connected to the inlet 2a of the carbon dioxide pump 2 through a pipeline; the outlet 2b of the carbon dioxide pump 2 is connected to the 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 to the inlet 4a of the carbon dioxide turbine 4 through a pipeline; the outlet 4b of the carbon dioxide turbine 4 is connected to the inlet 5a of the carbon dioxide condenser 5 through a pipeline; the outlet 5b of the carbon dioxide condenser 5 is connected to the inlet 1a of the carbon dioxide storage tank 1 through a pipeline; the rotating shaft of the carbon dioxide turbine 4 is connected to the input shaft of the generator 24.

In the organic Rankine cycle subsystem, the outlet 6b of the organic working fluid storage tank 6 is connected to the inlet 7a of the organic working fluid pump 7 through a pipeline; the outlet 7b of the organic working fluid pump 7 is connected to the cold source side inlet of the organic working fluid evaporator 8 through a pipeline; the cold source side outlet of the organic working fluid evaporator 8 is connected to the inlet 9a of the organic working fluid turbine 9 through a pipeline; the outlet 9b of the organic working fluid turbine 9 is connected to the inlet 10a of the organic working fluid condenser 10 through a pipeline; the outlet 10b of the organic working fluid condenser 10 is connected to the inlet 6a of the organic working fluid storage tank 6 through a pipeline; the rotating shaft of the organic working fluid turbine 9 is connected to the input shaft of the generator 25.

The outlet 23b of the heat exchange oil pump 23 is connected to the inlet of the internal heat exchanger IV of the medium-high temperature thermal energy chemical storage device 18 through a pipeline; the outlet of the internal heat exchanger IV of the medium-high temperature thermal energy chemical storage device 18 is connected to the heat source inlet of the organic working fluid evaporator 8 through a pipeline; the heat source outlet of the organic working fluid evaporator 8 is connected to 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 to the inlet 23a of the working fluid pump 23 through a pipeline.

A multi-cycle coupled power supply system with chemical quality improvement and heat storage, characterized in that the system is operated in the following steps:

First, the waste heat medium (such as water, flue gas, etc.) at 110℃-120℃ enters the internal heat exchanger I of the medium and low temperature waste heat chemical storage device 13 for heat exchange. After the heat exchange, the temperature of the waste heat medium is reduced and enters the medium and low temperature heat storage device 11 to further release heat, and then is discharged to the external environment.

Subsequently, the chemical quality improvement heat storage subsystem works, and the working process is divided into two stages: energy storage and energy release. In the energy storage stage, in the medium-low temperature waste heat storage unit, the chemical heat storage medium (hydrogen storage alloy NaAlH ₄ ) stored inside the medium-low temperature waste heat chemical storage device 13 absorbs heat from the waste heat medium through the internal heat exchanger I, and the hydrogen storage alloy NaAlH ₄ undergoes a forward endothermic decomposition reaction at a temperature of 105°C, and the reaction formula is:

ΔH＝37kJ/mol

ΔH＝37kJ/mol

The reaction generates hydrogen at about 105°C, and then the hydrogen enters the internal heat exchanger III of the endothermic reaction device 14 under the action of the compressor B for heat exchange. After the heat exchange, the temperature of the hydrogen decreases and enters the medium and low temperature heat storage device 11 to further release heat, and then is sent to the medium and low temperature product storage tank 12 through the compressor B for storage, thereby completing the medium and low temperature waste heat storage process.

In the energy storage stage, in the chemical heat pump upgrading unit, the chemical heat storage medium (liquid isopropanol) in the endothermic reaction device 14 absorbs heat from the hydrogen through the internal heat exchange III, and the liquid isopropanol absorbs heat and evaporates, and then a forward endothermic decomposition reaction occurs at a temperature of about 90° C. The catalyst is a ZnO/CuO composite catalyst, and the reaction formula is:

(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 at about 90°C. Subsequently, the acetone-hydrogen mixed gas at about 90°C and part of the unreacted gaseous isopropanol enter the distillation tower 15; in the distillation tower 15, according to the different boiling points of the acetone-hydrogen mixed gas and the gaseous isopropanol, most of the gaseous isopropanol is condensed and liquefied to be separated from the acetone-hydrogen mixed gas, and the liquid isopropanol obtained by condensation and liquefaction is then discharged back to the endothermic reaction device 14, the hydrogen-acetone mixed gas at about 80°C and a small amount of gaseous isopropanol that is not condensed and liquefied are discharged from the distillation tower 15 and enter the separation device 16; in the separation device 16, the remaining gaseous isopropanol is separated and discharged back to the distillation tower 15, and a high-purity acetone-hydrogen mixed gas at about 80°C is obtained. Subsequently, the high-purity acetone-hydrogen mixed gas at about 80°C enters the regenerator 17; in the regenerator 17, The high-purity acetone and hydrogen mixed gas at about 80°C absorbs heat and heats up to about 200°C, and then enters the internal reactor pipe of the medium-high temperature thermal energy chemical storage device 18; the internal reactor pipe of the medium-high temperature thermal energy chemical storage device 18 is filled with a solid catalyst Raney Ni, and the high-purity acetone and hydrogen mixed gas at about 200°C are catalyzed by the solid catalyst Raney Ni to undergo a reverse exothermic chemical reaction to generate gaseous isopropanol at about 250°C. The reaction formula is:

(CH ₃ ) ₂ CO(g)+H ₂ (g)→(CH ₃ ) ₂ CHOH(g) ΔH＝-55.0kJ/mol

The heat released by the reaction is absorbed by the reaction raw material hydrogen storage alloy _Mg2NiH4 filled outside the internal reactor pipe of the medium and _high temperature thermal energy chemical storage device 18, and then the gaseous isopropanol at about 250°C and the unreacted hydrogen and acetone mixed gas are discharged back to the regenerator 17; in the regenerator 17, the gaseous isopropanol at about 250°C and the unreacted hydrogen and acetone are heat exchanged with the high-purity acetone and hydrogen mixed gas at about 80°C from the separation device 16. After the heat exchange is completed, the temperature of the gaseous isopropanol at about 250°C and the unreacted hydrogen and acetone mixed gas drops to about 80°C and is discharged back to the endothermic reaction device 14, thereby completing the low-temperature waste heat quality upgrading process.

In the energy storage stage, in the medium-high temperature thermal storage unit, the filling reactant Mg ₂ NiH ₄ outside the internal reactor pipe of the medium-high temperature thermal energy chemical storage device 18 absorbs heat and gradually heats up, and a forward endothermic decomposition reaction occurs at a temperature of about 240°C. The reaction formula is:

Mg ₂ NiH ₄ (s)→Mg ₂ Ni(s)+2H ₂ (g) ΔH＝65kJ/mol

The reaction generates hydrogen at about 240°C, which is then discharged from the medium-high temperature thermal energy chemical storage device 18 under the suction action of the compressor A and enters the medium-high temperature heat storage device 19; the hydrogen at about 240°C is heat exchanged through the medium-high temperature heat storage device 19, and the heat of the hydrogen at about 240°C is stored in the medium-high temperature heat storage device 19. After the heat exchange is completed, the temperature of the hydrogen at about 240°C is reduced, and then it is sent to the medium-high temperature product storage tank 20 for storage through the compressor A, thereby completing the medium-high temperature thermal energy storage process.

In the energy release stage, in the medium and low temperature waste heat storage unit, the hydrogen in the medium and low temperature product storage tank 12 enters the medium and low temperature heat storage device 11 for heat exchange. After the heat exchange, the hydrogen is preheated to about 95°C and enters the medium and low temperature waste heat chemical storage device 13, and reacts with the original solid products Na ₃ AlH ₆ and Al at a temperature of 90°C in a reverse chemical reaction. The reaction formula is:

ΔH＝-37kJ/mol

ΔH＝-37kJ/mol

The released heat is used to heat domestic water through the internal heat exchanger II of the medium and low temperature waste heat chemical storage device 13 to complete the heating process; in the medium and high temperature heat storage unit, the hydrogen in the medium and high temperature product storage tank 20 enters the medium and high temperature heat storage device 19 for heat exchange. After the heat exchange is completed, the hydrogen is preheated to about 220°C and enters the medium and high temperature thermal energy chemical storage device 18, and reacts with the original solid product Mg ₂ Ni therein in a reverse chemical reaction at a temperature of about 220°C. 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 and high temperature thermal energy chemical storage device 18; during the peak period of electricity consumption, the heat exchange oil that absorbs heat passes through the organic working fluid evaporator 8 and the carbon dioxide evaporator 3 in sequence to heat the n-pentane and carbon dioxide; at the same time, the n-pentane in the organic working fluid storage tank 6 enters the organic working fluid pump 7 and is compressed to the set working pressure of 1.9Mpa, and the pressurized n-pentane is sent to the organic working fluid evaporator 8 to absorb heat. After absorbing heat, the n-pentane becomes superheated steam, and the superheated steam enters the organic working fluid turbine 9 to expand and do work. The organic working fluid turbine 9 rotates to drive the generator 25 to generate electricity. After doing work, the n-pentane is discharged from the organic working fluid turbine 9 and enters the organic working fluid condenser 10, where the condensation pressure is 0.1Mpa and the condensation temperature is 3 5℃, liquid n-pentane is pressurized and enters the organic working fluid evaporator 8 to continue absorbing the medium and high-grade thermal energy after the chemical upgrading and heat storage subsystem has upgraded the quality; the carbon dioxide in the carbon dioxide storage tank 1 enters the carbon dioxide pump 2 and is compressed to the set working pressure of 13Mpa, and the pressurized carbon dioxide is sent to the carbon dioxide evaporator 3 to absorb heat and become a supercritical state, and the supercritical carbon dioxide enters the carbon dioxide turbine 4 to expand and do work, and the carbon dioxide turbine 4 rotates to drive the generator 24 to generate electricity, and the carbon dioxide after doing work is discharged from the carbon dioxide turbine 4 and enters the carbon dioxide condenser 5 for condensation, and the condensed carbon dioxide is pressurized and enters the carbon dioxide evaporator 3 to continue absorbing the medium and high-grade thermal energy after the chemical upgrading and heat storage subsystem has upgraded the quality, thereby completing the power supply process.

In the embodiment, the medium and high-grade thermal energy upgraded by the chemical upgrading heat storage subsystem can also be coupled with other cycle power generation methods, such as: Kalina cycle, Brayton cycle, Stirling cycle, etc., not limited to the above-mentioned organic Rankine cycle and carbon dioxide cycle.

Finally, it should be noted that the above embodiments are only used to help understand the method and core idea of the present invention; at the same time, for those skilled in the art, according to the idea of the present invention, there will be changes in the specific implementation scheme and application scope. In summary, the content of the present invention description should not be understood as limiting the present invention.

Claims (2)

1. A multi-cycle coupled cogeneration system with chemical upgrading and heat storage, characterized in that: the system includes three subsystems, namely organic Rankine cycle subsystem, carbon dioxide cycle subsystem, chemical quality upgrading heat storage sub-system system; the chemical upgrading and thermal storage subsystem completes the upgrading and storage of external low-grade heat energy, and the chemical upgrading and thermal storage subsystem is connected in series with the organic Rankine cycle subsystem and the carbon dioxide cycle subsystem respectively through pipelines. The circulation subsystem and the carbon dioxide circulation subsystem use the medium and high-grade thermal energy upgraded by the chemical upgrading heat storage subsystem to generate electricity; The medium and low temperature waste heat storage unit of the chemical upgrading heat storage subsystem includes a medium and low temperature heat storage device (11), a medium and low temperature product storage tank (12), a medium and low temperature waste heat chemical storage device (13), and an endothermic reaction device (14), compressor B, valve two (22), the medium and low temperature waste heat chemical storage device (13) is filled with reaction raw materials based on the principle of chemical heat storage, the reaction raw materials can undergo forward endothermic reaction, and its reverse reaction It is an exothermic reaction; the chemical heat pump upgrading unit of the chemical upgrading heat storage sub-system includes an endothermic reaction device (14), a rectification tower (15), a separation device (16), a regenerator (17) and an intermediate A high-temperature thermal energy chemical storage device (18), the endothermic reaction device (14) is filled with reaction raw materials based on the principle of chemical heat storage, the reaction raw materials can undergo a forward endothermic reaction in a low-temperature environment, and a reverse reaction in a high-temperature environment reaction, the reverse reaction is an exothermic reaction; the medium-high temperature heat storage unit of the chemical upgrading heat storage subsystem includes a medium-high temperature thermal energy chemical storage device (18), a medium-high temperature heat storage device (19), a medium-high temperature product storage Tank (20), valve one (21) and compressor A, the interior of the medium-high temperature thermal energy chemical storage device (18) is filled with reaction raw materials based on the principle of chemical heat storage, the reaction raw materials can undergo forward endothermic reaction, and its reverse The reaction is exothermic; The organic Rankine cycle subsystem includes 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), generator two (25); The carbon dioxide circulation subsystem includes 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 one (24); In the chemical upgrading heat storage sub-system, the outlet of the internal heat exchanger I of the medium and low temperature waste heat chemical storage device (13) of the medium and low temperature waste heat storage unit passes through the pipeline and the heat source of the waste heat medium of the medium and low temperature heat storage device (11). The inlet (11d) is connected; the reaction product outlet of the medium and 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 endothermic reaction device (14) The outlet of the internal heat exchanger III is connected to the reaction product heat source inlet (11a) of the medium and low temperature heat storage device (11) through a pipeline; the reaction product outlet (11b) of the medium and low temperature heat storage device (11) is connected to the compressed air through a pipeline The inlet of the machine B is connected; the outlet of the compressor B is connected with the inlet of the medium and low temperature product storage tank (12) through a pipeline; the outlet of the medium and low temperature product storage tank (12) is connected through a pipeline, valve two (22) It is connected with the reaction product cold source inlet (11e) of the medium and low temperature heat storage device (11); the reaction product cold source outlet (11f) of the medium and low temperature heat storage device (11) is connected with the medium and low temperature waste heat chemical storage device (13 ) reaction product inlet connection; In the chemical upgrading heat storage subsystem, the reaction raw material-reaction product outlet (14a) of the endothermic reaction device (14) of the chemical heat pump upgrading unit passes through the pipeline and the reaction raw material-reaction product inlet of the rectification tower (15) (15a) is connected; the reaction raw material outlet (15d) of described rectification tower (15) is connected with the reaction raw material inlet (14c) of endothermic reaction device (14) by pipeline, the reaction raw material of rectification tower (15)-reaction Product outlet (15b) is connected with the reaction raw material-reaction product inlet (16a) of separation device (16) by pipeline; The reaction product outlet (16b) of described separation device (16) is through the reaction of pipeline and regenerator (17) The product inlet (17a) is connected, 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) by pipeline; The reaction raw material outlet of the described regenerator (17) ( 17d) Connect the reaction raw material inlet (14b) of the endothermic reaction device (14) through a pipeline, and the reaction product outlet (17b) of the regenerator (17) is connected to the internal reactor of the medium-high temperature thermochemical storage device (18) through a pipeline The pipeline inlet (18a) is connected; the internal reactor pipeline outlet (18b) of the medium-high temperature thermochemical storage device (18) is connected with the reaction raw material inlet (17c) of the regenerator (17) through a pipeline; In the carbon dioxide circulation subsystem, the outlet (1b) of the carbon dioxide storage tank (1) is connected with the inlet (2a) of the carbon dioxide pump (2) through a pipeline; the outlet (2b) of the carbon dioxide pump (2) is connected with the carbon dioxide through a pipeline The cold source side inlet of the evaporator (3) is connected; the cold source side outlet of the carbon dioxide evaporator (3) is connected with the inlet (4a) of the carbon dioxide turbine (4) through a pipeline; the outlet of the carbon dioxide turbine (4) ( 4b) connected to 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 pump storage tank (1) through a pipeline; the The rotating shaft of the carbon dioxide turbine (4) is connected with the input shaft of the generator one (24); In the organic Rankine cycle subsystem, the outlet (6b) of the organic working medium storage tank (6) is connected with the inlet (7a) of the organic working medium pump (7) through a pipeline; the organic working medium pump (7) The outlet (7b) is connected to the cold source side inlet of the organic working fluid evaporator (8) through a pipeline; the cold source side outlet of the organic working fluid evaporator (8) is connected to the inlet (9a) of the organic working fluid turbine (9) through a pipeline ) is connected; the outlet (9b) of the organic working medium turbine (9) is connected with the inlet (10a) of the organic working medium condenser (10) by 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 with the input shaft of the generator two (25); The outlet (23b) of the heat exchange oil pump (23) is connected with the inlet of the internal heat exchanger IV of the medium-high temperature thermochemical storage device (18) through a pipeline; the internal heat exchanger IV of the medium-high temperature thermochemical storage device (18) The outlet of is connected with the heat source inlet of organic working fluid vaporizer (8) by pipeline; The heat source outlet of described organic working fluid vaporizer (8) is connected with the heat source inlet of carbon dioxide vaporizer (3) by pipeline; The carbon dioxide vaporizer The heat source outlet of (3) is connected with the inlet (23a) of the heat exchange oil pump (23) through a pipeline. 2. A multi-cycle coupled cogeneration system with chemical upgrading and heat storage according to claim 1, characterized in that the system is carried out as follows: First, the waste heat-carrying medium with a certain temperature enters the internal heat exchanger I of the medium and low temperature waste heat chemical storage device (13) of the chemical upgrading and heat storage sub-system to exchange heat with the medium and low temperature heat storage device (11). After the temperature drops, discharged to the external environment; Subsequently, the chemical upgrading and thermal storage sub-system 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 and low temperature waste heat storage unit, the medium and low temperature waste heat chemical storage The stored reaction raw materials absorb the heat from the waste heat medium through the internal heat exchanger I, the reaction raw materials absorb heat and heat up, and a positive endothermic reaction occurs at a suitable temperature and pressure, and the reaction products include solid, gaseous or liquid. Then, according to the difference in the phase state and density of the product, the product is separated, and the solid product with high density is left in the medium and low temperature waste heat chemical storage device (13); the gaseous or liquid product with a certain temperature and low density enters The internal heat exchanger III of the endothermic reaction device (14) performs heat exchange. After the heat exchange, the temperature of the gaseous or liquid product with a certain temperature and low density decreases and enters the medium and low temperature heat storage device (11) to further release heat. The compressor B is sent to the medium and low temperature product storage tank (12) for storage, thereby completing the medium and low temperature waste heat storage process; In the energy storage stage, in the chemical heat pump upgrading unit, the reaction raw material inside the endothermic reaction device (14) absorbs the heat from the gaseous or liquid product with a certain temperature and low density through the internal heat exchanger III, and the reaction raw material Endothermic temperature rises, and positive endothermic reaction occurs under suitable temperature and pressure, and reaction product and part unreacted reaction raw material are transported to rectifying tower (15); In described rectifying tower (15), according to reaction Product and reaction raw material boiling point difference, reaction product is separated with reaction raw material, and most of reaction raw material with higher boiling point stays in rectifying tower (15), is discharged back to endothermic reaction device (14) subsequently, has certain Temperature and lower boiling point reaction products and a small amount of reaction raw materials are discharged from the rectification tower (15) and enter the separation device (16); in the separation device (16), the reaction raw materials and reaction products are further separated to obtain high-purity The reaction product, the separated reaction raw material is sent back to the rectification tower (15), and the high-purity reaction product enters the regenerator (17); in the described regenerator (17), the high-purity reaction product absorbs heat and heats up, Then it enters the internal reactor pipeline of the medium-high temperature thermochemical storage device (18); in the internal reactor pipeline of the medium-high temperature thermochemical storage device (18), the high-purity reaction product reversely discharges at a suitable temperature and pressure. Thermal reaction, the released heat is absorbed by the reaction raw materials filled outside the internal reactor pipeline of the medium-high temperature thermal energy chemical storage device (18), and at the same time, the reaction raw materials with a certain temperature and unreacted reaction products generated by the reverse exothermic reaction are transported to Regenerator (17); in the regenerator (17), the reaction raw materials with a certain temperature and the unreacted reaction product exchange heat with the high-purity reaction product from the separation device (16), after the heat exchange is completed The reaction raw materials with a certain temperature and the unreacted reaction products are lowered in temperature and transported to the endothermic reaction device (14), and the high-purity reaction products from the separation device (16) absorb heat and heat up and then enter the medium-high temperature thermal energy chemical storage device ( 18) internal reactor pipeline, thereby completing the low-temperature waste heat upgrading process; In the energy storage stage, in the medium-high temperature heat storage unit, the reaction raw materials filled outside the internal reactor pipe of the medium-high temperature thermal energy chemical storage device (18) absorb heat and heat up, and positive heat absorption occurs at a suitable temperature and pressure reaction, the reaction product contains solid, gaseous or liquid products, and then the products are separated according to the phase state and density of the products, and the solid products with high density are left in the medium-high temperature thermal energy chemical storage device (18), The gaseous or liquid product with a certain temperature and low density is discharged from the medium-high temperature thermal energy chemical storage device (18); the gaseous or liquid product with a certain temperature and low density passes through the medium-high temperature heat storage device (19) for heat exchange, The heat is stored in the medium-high temperature heat storage device (19). After the heat exchange is completed, the temperature of the gaseous or liquid product with a certain temperature and low density decreases, and is sent to the medium-high temperature product storage tank (20) through the compressor A. storage to complete the process of medium and high temperature thermal energy storage; In the energy release stage, in the medium and low temperature waste heat storage unit, the gaseous or liquid product in the medium and low temperature product storage tank (12) enters the medium and low temperature heat storage device (11) for heat exchange, and is preheated to a certain temperature After entering the medium and low temperature waste heat chemical storage device (13), a reverse exothermic reaction occurs with the original solid product in the medium and low temperature waste heat chemical storage device (13) at a suitable temperature and pressure, and the released heat is stored through the medium and low temperature waste heat chemical storage device. The internal heat exchanger II in the device (13) heats domestic water; at the same time, in the medium-high temperature heat storage unit, the gaseous or liquid product in the medium-high temperature product storage tank (20) is discharged, and passes through the medium-high temperature storage tank. The thermal device (19) performs heat exchange, and after being preheated to a certain temperature, it enters the medium-high temperature thermal energy chemical storage device (18), and forms a solid state with the original medium-high temperature thermal energy chemical storage device (18) The reverse exothermic reaction occurs; During the peak time of electricity consumption, the carbon dioxide circulation subsystem and the organic Rankine cycle subsystem start to work, and the heat exchange oil absorbs the heat released by the chemical reaction through the internal heat exchanger IV of the medium-high temperature thermal energy chemical storage device (18), and the temperature rises. The high heat exchange oil passes through the organic working medium evaporator (8) and the carbon dioxide evaporator (3) to heat the organic working medium and carbon dioxide successively; the organic working medium in the described organic working medium storage tank (6) enters the organic working medium pump ( 7) and be compressed to the set working pressure, the pressurized organic working fluid is sent to the organic working fluid evaporator (8) to absorb heat, the organic working fluid absorbs heat and becomes superheated steam, and the superheated steam in the organic working fluid The turbine (9) expands to do work, and the organic working medium turbine (9) rotates to drive the second generator (25) to generate electricity. After the work, the organic working medium is discharged from the organic working medium turbine (9) and enters the organic working medium condenser (10), the liquid organic working medium is pressurized and enters the organic working medium evaporator (8) to continue absorbing the medium and high-grade heat energy after the upgrading of the chemical upgrading heat storage subsystem; the carbon dioxide storage tank (1) Carbon dioxide enters the carbon dioxide pump (2) and is compressed to the set working pressure. The pressurized carbon dioxide is sent to the carbon dioxide evaporator (3) to absorb heat and become supercritical. The carbon dioxide is in the carbon dioxide turbine (4). The expansion works, the carbon dioxide turbine (4) rotates to drive the generator one (24) to generate electricity, the carbon dioxide after the work is discharged from the carbon dioxide turbine (4), enters the carbon dioxide condenser (5) to condense, and the condensed carbon dioxide is pressurized and enters The carbon dioxide evaporator (3) continues to absorb the medium and high-grade heat energy upgraded by the chemical upgrading heat storage subsystem to complete the power supply process.

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