阅读说明：本技术 一种基于太阳能利用的热-电-清洁水联产系统 (Heat-electricity-clean water co-production system based on solar energy utilization ) 是由 席奂 王美维 朱闯 陈晓弢 于 2020-08-06 设计创作，主要内容包括：一种基于太阳能利用的热-电-清洁水联产系统,将太阳能集热器采集的太阳辐射能分为三部分,一部分进入储能系统；一部分作为超临界布雷顿循环-热电联产子系统的能量来源；一部分作为超临界水氧化系统的能量来源,同时解决了用户的用电、用热和用水问题。本系统中的热负荷、电负荷及污水负荷相互耦合,互相影响,通过初始能量分配、子系统热力参数调整等方式,可实现整个系统电负荷、热负荷和污水负荷的协同控制,同时根据能量梯级原理对整个系统的低品位热量进行再利用,提高了系统能量利用率,并用CO<Sub>2</Sub>储气罐对CO<Sub>2</Sub>进行回收再利用,实现CO<Sub>2</Sub>零排放。且系统不是单一不可变的,由于子系统形式的多样性,可根据不同条件选择不同的子系统搭配方案。(A heat-electricity-clean water co-production system based on solar energy utilization divides solar radiation energy collected by a solar heat collector into three parts, and one part enters an energy storage system; one part is used as an energy source of the supercritical Brayton cycle-cogeneration subsystem; one part of the energy is used as an energy source of a supercritical water oxidation system, and the problems of electricity utilization, heat utilization and water utilization of users are solved at the same time. The heat load, the electric load and the sewage load in the system are mutually coupled and mutually influenced, the cooperative control of the electric load, the heat load and the sewage load of the whole system can be realized through the modes of initial energy distribution, subsystem thermal parameter adjustment and the like, and the low-grade heat of the whole system is recycled according to the energy step principle, so that the energy utilization rate of the system is improved, and CO is used 2 Gas storage tank pair CO 2 Recycling and reusing to realize CO 2 And (4) zero emission. And the system is not single and invariable, and different subsystem collocation schemes can be selected according to different conditions due to the diversity of subsystem forms.)

1. A combined heat-electricity-clean water production system based on solar energy utilization, comprising a solar heat collection device (29), characterized in that the outlet of the solar heat collection device (29) is divided into three flow paths:

the first one is connected with a heat storage device (24), the outlet of the heat storage device (24) is connected with a 3# working medium pump (23), and the 3# working medium pump (23) is connected with a solar heat collection device (29) to complete a cycle;

the second one is connected with a heat source side inlet of the supercritical water reactor (13), a heat source side outlet of the supercritical water reactor (13) is connected with a heat source side inlet of the 3# heat regenerator (20), a heat source side outlet of the 3# heat regenerator (20) is connected with a heat source side inlet of the 2# heat regenerator (19), a heat source side outlet of the 2# heat regenerator (19) is connected with a 3# working medium pump (23), and the 3# working medium pump (23) is connected with a solar heat collection device (29) to complete a cycle;

the third strip is connected with a heat source measuring port of the evaporator (25), a heat source measuring port of the evaporator (25) is connected with the 2# working medium pump (22), the 2# working medium pump (22) is connected with the 3# working medium pump (23), and the 3# working medium pump (23) is connected with the solar heat collecting device (29) to complete a cycle.

2. The combined heat-electricity-clean water generation system based on solar energy utilization according to claim 1, characterized in that the cold source side outlet of the evaporator (25) is connected with the inlet of the 3# expander (3), the outlet of the 3# expander (3) is connected with the heat source side inlet of the 4# regenerator (26), the heat source side outlet of the 4# regenerator (26) is connected with the heat source side inlet of the 5# regenerator (27), the heat source side outlet of the 5# regenerator (27) is divided into two branches, one branch is connected with the inlet of the 1# compressor (4), the outlet of the 1# compressor (4) is connected with the cold source side inlet of the 4# regenerator (26), the other branch is connected with the heat source side inlet of the 6# regenerator (28), the heat source side outlet of the 6# regenerator (28) is connected with the inlet of the 2# compressor (5), the outlet of the 2# compressor (5) is connected with the cold source side inlet of the 5# regenerator (27), and a cold source side outlet of the 5# heat regenerator (27) is connected with a cold source side inlet of the 4# heat regenerator (26), and a cold source side outlet of the 4# heat regenerator (26) is connected with a cold source side inlet of the evaporator (25) to complete a cycle, so that the supercritical Brayton cycle-cogeneration subsystem is formed.

3. The solar energy utilization based thermo-electric-clean water cogeneration system according to claim 2, characterized in that the # 2 compressor (5) can be a multi-stage compression-interstage cooling structure.

4. The solar energy utilization-based combined heat-electricity-clean water production system according to claim 2 or 3, wherein the 1# compressor (4) is a low-pressure compressor, the 2# compressor (5) is a high-pressure compressor, and the working medium of the supercritical Brayton cycle-combined heat and power production subsystem is supercritical CO₂，NH₃Or liquid nitrogen.

5. The solar energy utilization-based cogeneration system of heat, electricity and clean water according to claim 1, wherein the working medium inlet end of the supercritical water reactor (13) is connected to the working medium outlet of the heat regenerator # 1 (12), and the working medium inlet of the heat regenerator # 1 (12) is divided into two branches: the first one is connected with an oxidizing gas inlet through a multi-stage compression-interstage cooling structure, the second one is connected with a sewage buffer tank (10) through a booster pump (11), a slag discharge port of a supercritical water reactor (13) is connected with a slag storage tank (32), a cold source measuring port of the supercritical water reactor (13) is connected with an inlet of a 2# expansion machine (2), and an outlet of the 2# expansion machine (2)The inlet of the 2# condenser (21) is connected with the port, the exhaust heat of the 2# condenser (21) is supplied to a heat user, the outlet of the 2# condenser is connected with a gas-liquid separation device (16), the gas outlet of the gas-liquid separation device (16) is connected with a gas separation device (15), and CO is completed in the gas separation device (15)₂The liquid outlet of the gas-liquid separation device (16) is a clean water outlet, thereby forming the SCWO subsystem.

6. The solar energy utilization-based thermo-electric-clean water cogeneration system according to claim 5, wherein the multi-stage compression-interstage cooling structure II comprises a 3# compressor (6), wherein an outlet of the 3# compressor (6) is connected with a working medium inlet of a 1# regenerator (12), an inlet of the 3# compressor (6) is connected with a 4# condenser (31), an inlet of the 4# condenser (31) is connected with an outlet of a 4# compressor (7), an inlet of the 4# compressor (7) is connected with an oxidizing gas inlet, the booster pump (11) is connected with a gas outlet of the 5# compressor (8), and an inlet of the 5# compressor (8) is connected with the oxidizing gas inlet; the medium outlet of the No. 1 regenerator (12) is connected with the cold source side inlet of the No. 3 regenerator (20), the medium inlet of the No. 1 regenerator (12) is connected with the cold source side outlet of the No. 3 regenerator (20), and the No. 1 regenerator (12) and the No. 3 regenerator (20) absorb heat and emit heat one by one to complete one cycle.

7. The solar energy utilization-based thermo-electric-clean water cogeneration system according to claim 1, characterized in that the cold source side inlet of the # 2 regenerator (19) is connected with the outlet of the # 1 working medium pump (17), the cold source side outlet of the # 2 regenerator (19) is connected with the inlet of the # 1 expansion machine (1), the outlet of the # 1 expansion machine (1) is connected with the inlet of the # 1 condenser (18), the exhausted heat of the # 1 condenser (18) is supplied to a heat user, and the outlet of the # 1 expansion machine is connected with the inlet of the # 1 working medium pump (17) to complete a cycle, so that an ORC subsystem is formed, and the working medium of the ORC subsystem is R123, R245fa or R134a, or a mixed working medium formed by mixing more than two pure organic matters.

8. The solar energy utilization-based thermo-electric-clean water cogeneration system according to claim 7, characterized in that a shared regenerator (ambiguous) is added between the 1# expansion machine (1) and the 1# condenser (18) and between the 1# working medium pump (17) and the 2# regenerator (19) (same as the first patent, the regenerator has two inlet ends, one inlet end is added, and one cold source and one heat source are added in total), the exhaust steam of the 1# expansion machine (1) and the liquid working medium pressurized by the 1# working medium pump (17) are respectively introduced into the regenerator, the liquid working medium is heated by the exhaust steam of the 1# expansion machine (1) and then enters the 2# regenerator (19), and the exhaust steam of the 1# expansion machine (1) is cooled by the liquid working medium and then enters the 1# condenser (18).

9. A combined heat-electricity-clean water generation system based on solar energy utilization according to claim 1, characterized in that each expander and compressor is coaxially connected to the power plant (9).

Technical Field

The invention belongs to the technical field of energy utilization, relates to the fields of supercritical water oxidation and organic Rankine cycle, and particularly relates to a heat-electricity-clean water co-production system based on solar energy utilization.

Background

The present combined heat and power generation technology that mainly is thermal power plant satisfies user's power consumption and heat demand, but thermal power plant burning coal has aggravated the burden of environment, it is the hot spot down to study clean energy and satisfy user's demand, the application of solar thermal energy electricity combined heat generation technology is when solving user's demand, also not cause the influence to the environment, but the present utilization to solar thermal energy that heat collection device absorbed in the solar thermal energy electricity combined heat generation system has not been perfect yet, some low-grade energy do not recycle, it is extravagant to have caused the unnecessary energy.

The treatment of industrial sewage is always concerned by society, with the rapid increase of industrial sewage discharge, the traditional sewage treatment technology is difficult to meet the requirements of sewage treatment in terms of efficiency and technology, and the supercritical water oxidation technology can deeply oxidize various organic matters in the industrial sewage to convert the organic matters into clean water and CO₂And inorganic salts in which the relevant elements are stable. The supercritical oxidation technology for treating sewage has the characteristics of high efficiency and cleanness. And traditional sewage treatment technology does not rationally utilize a large amount of chemical energy that organic matter contained in the waste water, and these chemical energy will release a large amount of heat energy in the oxidation process at supercritical water oxidation in-process, and the rational utilization these heat energy can increase the utilization ratio of the energy.

Energy utilization is very important, and enterprises and society benefit badly if some energy which seems to be less affected can be effectively utilized under the improvement of management technology. At present, solar energy is mainly used for generating electricity, the solar energy is finally converted into electric energy to be provided for users, and a large amount of energy is wasted because the energy is not utilized in a gradient manner. Meanwhile, in the current treatment process of industrial sewage, the traditional sewage treatment technology has no advantages of cleanness, high efficiency and the like, and the high-efficiency technology of supercritical water oxidation cannot well utilize a large amount of organic chemical energy in the sewage. In both cogeneration and sewage treatment, some low-grade heat is not reasonably utilized, so that unnecessary energy is wasted.

Disclosure of Invention

In order to overcome the defects of the prior art, the invention aims to provide a heat-electricity-clean water cogeneration system based on solar energy utilization, which carries out overall management on energy in solar heat and electricity cogeneration and energy in supercritical water oxidation, couples and influences heat load, electric load and sewage load of the system, and realizes cooperative control of the electric load, the heat load and the sewage load of the whole system by means of initial energy distribution, subsystem thermal parameter adjustment and the like. And uses the principle of energy cascade utilization to treat some low productsReuse of heat energy, CO₂Also can be recycled to realize CO₂And (4) zero emission. Meanwhile, the energy problem and the sewage treatment problem are solved, and the power consumption, water consumption and heat consumption problems of users are met.

In order to achieve the purpose, the invention adopts the technical scheme that:

a combined heat-electricity-clean water generation system based on solar energy utilization, comprising a solar heat collection device 29, wherein the outlet of the solar heat collection device 29 is divided into three flow paths:

the first one is connected with a heat storage device 24, the outlet of the heat storage device 24 is connected with a 3# working medium pump 23, and the 3# working medium pump 23 is connected with a solar heat collection device 29 to complete a cycle;

the second is connected with a heat source side inlet of the supercritical water reactor 13, a heat source side outlet of the supercritical water reactor 13 is connected with a heat source side inlet of the 3# heat regenerator 20, a heat source side outlet of the 3# heat regenerator 20 is connected with a heat source side inlet of the 2# heat regenerator 19, a heat source side outlet of the 2# heat regenerator 19 is connected with the 3# working medium pump 23, and the 3# working medium pump 23 is connected with the solar heat collection device 29 to complete a cycle;

the third is connected with the heat source measuring port of the evaporator 25, the heat source measuring port of the evaporator 25 is connected with the 2# working medium pump 22, the 2# working medium pump 22 is connected with the 3# working medium pump 23, and the 3# working medium pump 23 is connected with the solar heat collecting device 29 to complete a cycle.

The cold source side outlet of the evaporator 25 is connected with the inlet of the 3# expansion machine 3, the outlet of the 3# expansion machine 3 is connected with the heat source side inlet of the 4# heat regenerator 26, the heat source side outlet of the 4# heat regenerator 26 is connected with the heat source side inlet of the 5# heat regenerator 27, the heat source side outlet of the 5# heat regenerator 27 is divided into two branches, one branch is connected with the inlet of the 1# compressor 4, the outlet of the 1# compressor 4 is connected with the cold source side inlet of the 4# heat regenerator 26, the other branch is connected with the heat source side inlet of the 6# heat regenerator 28, the heat source side outlet of the 6# heat regenerator 28 is connected with the inlet of the 2# compressor 5, the outlet of the 2# compressor 5 is connected with the cold source side inlet of the 5# heat regenerator 27, the cold source side outlet of the 5# heat regenerator 27 is connected with the cold source side inlet of the 4# heat regenerator 26, and the cold source side outlet of, thereby forming a supercritical brayton cycle-cogeneration subsystem.

The # 2 compressor 5 may be a multi-stage compression-interstage cooling structure.

The 1# compressor 4 is a low-pressure compressor, the 2# compressor 5 is a high-pressure compressor, and the working medium of the supercritical Brayton cycle-combined heat and power generation subsystem is supercritical CO₂，NH₃Or liquid nitrogen.

The working medium inlet end of the supercritical water reactor 13 is connected with the working medium outlet of the 1# heat regenerator 12, and the working medium inlet of the 1# heat regenerator 12 is divided into two branches: the first one is connected with an oxidizing gas inlet through a multi-stage compression-interstage cooling structure, the second one is connected with a sewage buffer tank 10 through a booster pump 11, a slag discharge port of a supercritical water reactor 13 is connected with a slag storage tank 32, a cold source measuring port of the supercritical water reactor 13 is connected with an inlet of a 2# expansion machine 2, an outlet of the 2# expansion machine 2 is connected with an inlet of a 2# condenser 21, heat discharge of the 2# condenser 21 is supplied to a heat user, an outlet of the 2# condenser is connected with a gas-liquid separation device 16, a gas outlet of the gas-liquid separation device 16 is connected with a gas separation device 15, and CO is completed in the gas separation device₂The liquid outlet of the gas-liquid separation device 16 is a clean water outlet, thereby forming an SCWO subsystem.

The second multi-stage compression-interstage cooling structure comprises a 3# compressor 6, wherein the outlet of the 3# compressor 6 is connected with the working medium inlet of a 1# heat regenerator 12, the inlet of the 3# compressor 6 is connected with a 4# condenser 31, the inlet of the 4# condenser 31 is connected with the outlet of a 4# compressor 7, the inlet of the 4# compressor 7 is connected with an oxidizing gas inlet, the booster pump 11 is connected with the gas outlet of a 5# compressor 8, and the inlet of the 5# compressor 8 is connected with the oxidizing gas inlet; the medium outlet of the 1# thermal regenerator 12 is connected with the cold source side inlet of the 3# thermal regenerator 20, the medium inlet of the 1# thermal regenerator 12 is connected with the cold source side outlet of the 3# thermal regenerator 20, and the 1# thermal regenerator 12 and the 3# thermal regenerator 20 absorb heat and emit heat one by one to complete one cycle.

The cold source side inlet of the 2# heat regenerator 19 is connected with the outlet of the 1# working medium pump 17, the cold source side outlet of the 2# heat regenerator 19 is connected with the inlet of the 1# expansion machine 1, the outlet of the 1# expansion machine 1 is connected with the inlet of the 1# condenser 18, the heat exhaust of the 1# condenser 18 is supplied to a heat user, the outlet of the 1# condenser is connected with the inlet of the 1# working medium pump 17 to complete one cycle, therefore, an ORC subsystem is formed, and the working medium of the ORC subsystem is R123, R245fa or R134a or a mixed working medium formed by mixing more than two pure organic matters.

In the ORC subsystem, a shared heat regenerator is added between a 1# expansion machine 1 and a 1# condenser 18 and between a 1# working medium pump 17 and a 2# heat regenerator 19, the difference is the same as that of the first patent, the heat regenerator is provided with two inlet ends, only one heat source is added, namely one cold source and one heat source, exhaust steam of the 1# expansion machine 1 and liquid working medium pressurized by the 1# working medium pump 17 are respectively introduced into the heat regenerator, the liquid working medium is heated by the exhaust steam of the 1# expansion machine 1 and then enters the 2# heat regenerator 19, and the exhaust steam of the 1# expansion machine 1 is cooled by the liquid working medium and then enters the 1# condenser 18.

The expanders and compressors of the present invention are all coaxially connected to the power plant 9.

Compared with the prior art, the invention utilizes the energy cascade utilization principle to recycle the low-grade energy in reactants of the whole system including a solar energy utilization system and a supercritical water oxidation system and in a supercritical Brayton cycle and to recycle CO₂The recycling is carried out, and the effects of energy conservation and environmental protection are achieved. And the ORC system and the supercritical brayton cycle cogeneration both have different forms, and are not single, and different collocation schemes can be selected according to different requirements, for example, the collocation scheme of the ORC system with a heat regenerator and the supercritical brayton cycle cogeneration system adopting single-machine compression, or the collocation scheme of the ORC system without a heat regenerator and the supercritical brayton cycle cogeneration system adopting multi-stage compression, and the like.

Drawings

FIG. 1 is a schematic view of the structure of the present invention

Wherein, 1 is a 1# expander, 2 is a 2# expander, 3 is a 3# expander, 4 is a 1# compressor, 5 is a 2# compressor, 6 is a 3# compressor, 7 is a 4# compressor, 8 is a 5# compressor, 9 is power generation equipment, 10 is a sewage buffer tank, 11 is a booster pump, 12 is a 1# heat regenerator, 13 is a supercritical water reactor, 14 is CO₂A storage tank, 15 is a gas separation device, 16 is a gas-liquid separation device, 17 is a # 1 working medium pump, 18 is a # 1 condenser, 19 is a # 2 regenerator, 20 is a # 3 regenerator, 21 is a # 2 condenser, 22 is a # 2 working medium pump, and 23 is a # 3 condenserThe heat storage device comprises a # working medium pump, a # working medium pump 24, an evaporator 25, a # 4 regenerator 26, a # 5 regenerator 27, a # 3 condenser 28, a solar heat collection device 29, a heliostat 30, a # 4 condenser 31 and a slag storage tank 32.

Detailed Description

The embodiments of the present invention will be described in detail below with reference to the drawings and examples.

As shown in fig. 1, a cogeneration system of heat-electricity-clean water based on solar energy utilization comprises a solar heat collection device 29, wherein the outlet of the solar heat collection device 29 is divided into three flow paths:

the first one is connected with a heat storage device 24, the outlet of the heat storage device 24 is connected with a No. 3 working medium pump 23, and the No. 3 working medium pump 23 is connected with a solar heat collection device 29 to complete a cycle.

The second is connected with a heat source side inlet of the supercritical water reactor 13, a heat source side outlet of the supercritical water reactor 13 is connected with a heat source side inlet of the 3# heat regenerator 20, a heat source side outlet of the 3# heat regenerator 20 is connected with a heat source side inlet of the 2# heat regenerator 19, a heat source side outlet of the 2# heat regenerator 19 is connected with the 3# working medium pump 23, and the 3# working medium pump 23 is connected with the solar heat collection device 29 to complete one cycle.

The third is connected with the heat source measuring port of the evaporator 25, the heat source measuring port of the evaporator 25 is connected with the 2# working medium pump 22, the 2# working medium pump 22 is connected with the 3# working medium pump 23, and the 3# working medium pump 23 is connected with the solar heat collecting device 29 to complete a cycle.

The co-production system of the present invention requires the use of multiple stages of expanders, illustrated as three stages of expanders, designated as expander 1, 2# 2 and 3# 3, respectively.

Wherein, the cold source side outlet of the evaporator 25 is connected with the inlet of the 3# expansion machine 3, the outlet of the 3# expansion machine 3 is connected with the heat source side inlet of the 4# heat regenerator 26, the heat source side outlet of the 4# heat regenerator 26 is connected with the heat source side inlet of the 5# heat regenerator 27, the heat source side outlet of the 5# heat regenerator 27 is divided into two branches, one branch is connected with the inlet of the 1# compressor 4, the outlet of the 1# compressor 4 is connected with the cold source side inlet of the 4# heat regenerator 26, the other branch is connected with the heat source side inlet of the 6# heat regenerator 28, the heat source side outlet of the 6# heat regenerator 28 is connected with the inlet of the 2# compressor 5, the outlet of the 2# compressor 5 is connected with the cold source side inlet of the 5# heat regenerator 27, the cold source side outlet of the 5# heat regenerator 27 is connected with the cold source side inlet of the 4# heat regenerator 26, the cold source side outlet of, thereby forming a supercritical brayton cycle-cogeneration subsystem.

In the present invention, the # 2 compressor 5 may be a multi-stage compression-inter-stage cooling structure, and the present embodiment employs single-stage compression.

The working medium inlet end of the supercritical water reactor 13 is connected with the working medium outlet of the 1# heat regenerator 12, and the working medium inlet of the 1# heat regenerator 12 is divided into two branches: the first one is connected with an oxidizing gas inlet through a multi-stage compression-interstage cooling structure, the second one is connected with a sewage buffer tank 10 through a booster pump 11, a slag discharge port of a supercritical water reactor 13 is connected with a slag storage tank 32, a cold source measuring port of the supercritical water reactor 13 is connected with an inlet of a 2# expansion machine 2, an outlet of the 2# expansion machine 2 is connected with an inlet of a 2# condenser 21, heat discharge of the 2# condenser 21 is supplied to a heat user, an outlet of the 2# condenser is connected with a gas-liquid separation device 16, a gas outlet of the gas-liquid separation device 16 is connected with a gas separation device 15, and CO is completed in the gas separation device₂The liquid outlet of the gas-liquid separation device 16 is a clean water outlet, thereby forming an SCWO subsystem.

Specifically, the second multi-stage compression-interstage cooling structure in the embodiment adopts two-stage compression, and includes a 3# compressor 6 and a 4# compressor 7, an outlet of the 3# compressor 6 is connected with a working medium inlet of a 1# regenerator 12, an inlet of the 3# compressor 6 is connected with a 4# condenser 31, an inlet of the 4# condenser 31 is connected with an outlet of the 4# compressor 7, an inlet of the 4# compressor 7 is connected with an oxidizing gas inlet, a booster pump 11 is connected with a gas outlet of the 5# compressor 8, and an inlet of the 5# compressor 8 is connected with an oxidizing gas inlet; the medium outlet of the 1# regenerator 12 is connected with the cold source side inlet of the 3# regenerator 20, the medium inlet of the 1# regenerator 12 is connected with the cold source side outlet of the 3# regenerator 20, and the 1# regenerator 12 and the 3# regenerator 20 absorb heat and emit heat one by one to complete one cycle.

The inlet of the cold source side of the 2# heat regenerator 19 is connected with the outlet of the 1# working medium pump 17, the outlet of the cold source side of the 2# heat regenerator 19 is connected with the inlet of the 1# expansion machine 1, the outlet of the 1# expansion machine 1 is connected with the inlet of the 1# condenser 18, the heat exhaust of the 1# condenser 18 is supplied to a heat user, and the outlet of the heat exhaust is connected with the inlet of the 1# working medium pump 17 to complete one cycle, so that an ORC subsystem is formed.

In the ORC subsystem, a shared heat regenerator is added between a 1# expansion machine 1 and a 1# condenser 18 and between a 1# working medium pump 17 and a 2# heat regenerator 19, the ambiguity is the same as that of a first patent, the heat regenerator is two inlet ends of two inlet ends, only one heat source is added, one cold source and one heat source are added, exhaust steam of the 1# expansion machine 1 and liquid working medium pressurized by the 1# working medium pump 17 are respectively introduced into the heat regenerator, the liquid working medium is heated by the exhaust steam of the 1# expansion machine 1 and then enters the 2# heat regenerator 19, and the exhaust steam of the 1# expansion machine 1 is cooled by the liquid working medium and then enters the 1# condenser 18.

In the invention, the solar heat collection device 29 absorbs sunlight reflected by the heliostat 30 to convert solar energy into heat energy, heat conduction oil is used as an energy transportation carrier, and the heat conduction oil can be replaced by other working media meeting the requirements of working conditions.

In the present invention, the 1# expander 1, the 2# expander 2, the 3# expander 3, the 1# compressor 4, the 2# compressor 5, the 3# compressor 6, the 4# compressor 7, and the 5# compressor 8 are coaxially connected to the power generation equipment 9, and the compressors are driven to operate by the output power of the multistage expander, and the excess output power is inputted to the power generation equipment 9 to generate power. The booster pump 11 for boosting the sewage is driven by the 5# compressor 8.

In the supercritical Brayton cycle-CHP subsystem, the working medium can adopt supercritical CO₂、NH₃Or liquid nitrogen and other working media meeting the requirements of working conditions, and CO is used in the invention₂The description is given.

In the organic Rankine cycle, working media meeting working condition requirements, such as R123, R245fa or R134a, or mixed working media meeting working condition requirements, which are formed by mixing two or more pure organic matters, can be adopted, and the working media are uniformly represented by the working media.

The invention is provided with a two-way valve and a three-way valve on each pipeline and between the pipelines, can be electromagnetic and is provided with a radio frequency control device; each working medium pump and each booster pump can be provided with a frequency conversion facility and a radio frequency control device.

On the basis, the energy utilization mechanism of the invention is as follows:

the heat transfer oil releases heat to the supercritical water oxidation reactor 1, then passes through the 3# heat regenerator 20 and the 2# heat regenerator 19 in sequence, provides the heat to reactants in the ORC subsystem and the SCWO system, and completes the utilization of low-grade energy.

CO from # 5 regenerator 27₂The heat energy is divided into two parts, one part flows into the 3# condenser 28 to provide heat energy for users, then flows into the 2# compressor 5 for compression, then flows into the 5# heat regenerator 27 for heat absorption, then flows into the 4# heat regenerator 26 for heat absorption, and the other part flows into the 1# compressor 1 for compression and then flows into the 4# heat regenerator 26 and the front CO₂Mixing, and controlling the energy distribution of the two parts to solve the heat consumption problem of users and finish the utilization of low-grade energy.

Working media from the supercritical water oxidation reactor sequentially pass through the 2# expansion machine 2 and the 2# condenser 21, energy is converted into electric energy and heat energy to be provided for users, and low-grade energy is utilized;

CO is arranged behind the gas separation device 15₂A buffer tank 14 for CO generated by the reaction in the supercritical water oxidation system₂The recovered CO can be applied to a supercritical Brayton-cogeneration system as a working medium for CO₂Reuse to realize CO₂And (4) zero emission.

In the ORC subsystem, a shared heat regenerator can be added between the 1# expansion machine 1 and the 1# condenser 18 and between the 1# working medium pump 17 and the 2# heat regenerator 19, the exhaust steam of the 1# expansion machine 1 and the liquid working medium pressurized by the 1# working medium pump 17 are respectively introduced into the heat regenerator, the liquid working medium enters the 2# heat regenerator 19 after being heated by the exhaust steam of the 1# expansion machine 1, the exhaust steam of the 1# expansion machine 1 enters the 1# condenser 18 after being cooled by the liquid working medium, and the energy loss of the system is reduced.

In the supercritical brayton cycle system, the 2# compressor 5 can adopt a multi-stage compression and interstage cooling method, and by taking the two-stage compressor as an illustration, a part of working medium flowing out of the 5# heat regenerator 27 is pre-cooled by the 3# condenser 28, then compressed by the two-stage compressor (low-pressure compressor-condenser intercooling-high-pressure compressor), flows into the 5# heat regenerator 27 to absorb heat, and then flows into the 4# heat regenerator 26 to absorb heat, and the flow of other working media is unchanged, which is the same as the description above. When heat supply is not needed, the circulation efficiency can be effectively improved by adopting a shunting and multistage compression method.

The working principle and the using steps of the invention are further explained in the following with the attached drawings:

as shown in fig. 1, the solar heat collection device 29 absorbs sunlight reflected by the heliostat 30, the heat conduction oil is used as a transport carrier to convert solar energy into heat energy, the two-way valve is opened to input the heat conduction oil into the system, the three-way valve can control a part of the heat conduction oil to enter the heat storage device 24 to store abundant solar energy, or the solar energy is stored when the load of other subsystems is small, so that the change of rainy weather, night and season is ensured, the system can meet the requirements of electric load and heat load, and when the load is required, the 3# working medium pump 23 brings the heat conduction oil in the heat storage device 24 into the solar heat collection device 29 and redistributes the heat conduction oil into the system; the three-way valve is controlled to transport part of heat conduction oil to the supercritical water reactor 13 to serve as an energy source of the SCWO system, part of heat of the heat conduction oil in the supercritical water reactor 13 is utilized, the energy is reduced after flowing out, the heat is released through the 3# heat regenerator 20, the released heat is absorbed by the 1# heat regenerator 12 and is supplied to reactants of the SCWO system, the heat conduction oil flows out of the 3# heat regenerator 20 and is released through the 2# heat regenerator 19, the heat is supplied to the ORC subsystem to serve as the energy source of the heat, finally, the heat flows through the 3# working medium pump 23 and returns to the solar heat collection device 29, the next cycle is started, and the 3# working medium pump 23 drives the heat conduction oil to circulate to flow and controls the; controlling a three-way valve to transport part of the heat transfer oil to the supercritical CO₂In the evaporator 25, heat is released, the part of energy is provided for an energy source of a supercritical Brayton cycle-CHP subsystem, then flows through a 2# working medium pump 22 and a 3# working medium pump 23 in sequence, finally returns to a solar heat collection device 29, and starts the next cycle, the 2# working medium pump 22 can control to flow through supercritical CO₂The flow rate of the evaporator 25 is controlled to control the energy supply of the critical brayton cycle.

In the SCWO system, air enters the system and then is divided into two parts, one part of air pushes a No. 5 compressor 8, the No. 5 compressor 8 drives a booster pump 11, and the air is fed into a sewage buffer tank 10The sewage pressurization of outflow, reach the pressure condition of supercritical water oxidation reaction, in order to save the consumption of compressor, another part air gets into 4# compressor 7 compression earlier, the air that 4# compressor 7 flows out is at first through 4# condenser 31 cooling, compress through 3# compressor 6 again, then mix with the sewage that booster pump 11 flows out and get into 1# regenerator 12, absorb the heat, the heat that releases 3# regenerator 20 is recycled, make the reactant reach high temperature high pressure, accord with the reaction condition of supercritical water oxidation, the emergence reaction in the supercritical water reactor 13 of entering. Solid inorganic salt and other heavy metal solid phases generated by the reaction are discharged into a slag storage tank 32 for treatment, high-temperature and high-pressure gas generated by the reaction enters a 2# expansion machine 2 through a pipeline to do work, then the heat is released through a 2# condenser 21, water vapor is condensed into liquid water, the heat released can solve the heat consumption problem of a user, gas and water discharged from the 2# condenser 21 are separated in a gas-liquid separation device 16, the water at the moment can solve the water consumption problem of the user after being treated by a supercritical water oxidation technology, the liquid is separated through a gas separation device 15, and CO in the generated substances is separated₂Discharge to CO₂The gas in the storage tank 14 is reused and can be used as working medium of other subsystems or for other purposes, and other separated gas is N₂And the like, and is discharged into the atmosphere.

In the ORC subsystem, working medium is compressed and driven by a 1# working medium pump 17, low-grade heat of heat conducting oil flowing out of a supercritical water reactor 13 is recycled through a 2# heat regenerator 19, the heat is absorbed and then enters a 1# expansion machine 1 to do work through expansion, the output work of the 1# expansion machine 1 is used for driving the power generation of a compressor and power generation equipment in the system, then the heat is released by entering a 1# condenser 18, the heat generated can solve the heat utilization problem of a user, and the working medium returns to the 1# working medium pump 17 after flowing out of the 1# condenser 18 and starts the next cycle. Meanwhile, as a preferred embodiment, a shared heat regenerator can be added between the 1# expansion machine 1 and the 1# condenser 18 and between the 1# working medium pump 17 and the 2# heat regenerator 19, the exhaust steam of the 1# expansion machine 1 and the liquid working medium pressurized by the 1# working medium pump 17 are respectively introduced into the heat regenerator, the liquid working medium enters the 2# heat regenerator 19 after being heated by the exhaust steam of the 1# expansion machine 1, and the exhaust steam of the 1# expansion machine 1 enters the 1# condenser 18 after being cooled by the liquid working medium.

CO in a supercritical Brayton cycle-cogeneration subsystem₂Working fluids, e.g. higher pressure CO₂The heat absorbed by heat conducting oil in the evaporator 25 reaches a supercritical state, the heat enters the 3# expansion machine 3 to do work, the output work of the 3# expansion machine 3 is used for driving the compressor and the power generation equipment in the system to generate power, then the heat enters the 4# heat regenerator 26 and the 5# heat regenerator 27 in sequence to release heat, the working medium coming out of the 5# heat regenerator 27 is divided into two flow channels, one part of the working medium flows through the 1# compressor 4 to increase the compression pressure, the other part of the working medium flows through the 3# condenser 28 to cool and release heat, the heat is provided for users, then flows through the 2# compressor 5 to increase the compression pressure, and then flows into the 5# heat regenerator 27 to absorb the heat emitted in the front, after the two working media are completed, the two working media are mixed and enter the 4₂And back to the high pressure state, and back to the evaporator 25 to start the next cycle. The present invention can adjust the flow rate into the # 3 condenser 28 according to the amount of heat required by the user. Meanwhile, in order to meet the situation that a user does not have a heat demand, in order to improve the cycle efficiency, the 2# compressor 5 can adopt a multi-stage compression and interstage cooling method, the two-stage compressor is taken as an illustration, a part of working medium flowing out of the 5# heat regenerator 27 is pre-cooled by the 3# condenser 28, compressed by the two-stage compressor (low-pressure compressor-condenser intercooling-high-pressure compressor), flows into the 5# heat regenerator 27 to absorb heat, then flows into the 4# heat regenerator 26 to absorb heat, and the flow of other working media is unchanged, which is the same as the illustration.

In the invention, the change of certain parameters can affect the whole system, for example, the change of sewage flow can directly influence the power of the supercritical reactor 13, so that the energy entering the supercritical Brayton cycle-combined heat and power generation subsystem through the evaporator 25 is changed, the output power of the expander 3 is changed while the change of the output power of the expander 2 is influenced, the variability of the system is fully shown, because the electric load, the heat load and the sewage load of each subsystem are influenced mutually, the invention can adjust the distribution of initial energy and adjust the thermodynamic parameters of the subsystems according to different requirements to realize the cooperative control of the electric load, the heat load and the sewage load of the whole system, and because each subsystem accords with the diversity of working media of working conditions, the form of an ORC system and the diversity of the form of the supercritical Brayton cycle combined heat and power generation system, the selection of the whole system is more comprehensive, and different requirements can be met.

In summary, the invention stores a part of the heat energy converted by solar energy as a standby, a part of the heat energy is used as an energy source of a supercritical Brayton cycle-CHP, and a part of the heat energy is used as an energy source of a supercritical water oxidation system. Solar energy utilization and sewage treatment are combined, a supercritical Brayton cycle-CHP subsystem, an SCWO subsystem and an ORC-CHP subsystem are coupled and managed in a unified mode, power output of the subsystems is coordinated and controlled through adjusting parameters, the subsystems affect each other, sewage is treated in a high-efficiency and clean mode through a supercritical water oxidation technology, solar energy is distributed reasonably, and meanwhile the problems of electricity utilization, heat utilization and water utilization of users are solved.