A hydrogen and electricity cogeneration system and method for organic solid waste combustion and gasification

Abstract

The present application relates to the field of organic solid waste resource utilization and hydrogen energy technology, and particularly relates to a hydrogen and heat cogeneration system and method for organic solid waste combustion and gasification. In the present application, the organic solid waste is divided into high-calorific-value organic solid waste and low-calorific-value organic solid waste based on calorific value and water content. The high-calorific-value organic solid waste is calcined with limestone, and the low-calorific-value organic solid waste is used for gasification. The present application ensures that the organic solid waste with different calorific values and water contents is fully digested, and solves the problem of unstable operation caused by the complex composition of organic solid waste. A three-stage energy cascade utilization module is constructed, and the traditional single power generation and single heat supply mode is innovated into a heat, electricity and hydrogen energy cogeneration mode. A calcium-based material circulation system is systematically constructed, and the "hydrogen production-pollution control" integration is realized. The present application has significant economic and environmental benefits, and provides a solution for high-value utilization of organic solid waste and green hydrogen production.

Description

TECHNICAL FIELD

[0001] The present application relates to the technical field of organic solid waste resource utilization and hydrogen energy, and particularly relates to a hydrogen-electricity-heat cogeneration system and method for organic solid waste combustion and gasification. BACKGROUND

[0002] The information disclosed in this BACKGROUND section is only for the purpose of increasing the understanding of the background of the present application and should not be taken as an acknowledgement or any form of suggestion that this information forms prior art that is publicly known.

[0003] With the progress of society and economic development, clean energy utilization is increasingly valued by people. At present, the demand for energy is strong, and the contradiction between supply and demand is prominent. Moreover, in the process of energy utilization, there are problems such as unreasonable energy utilization structure, low energy utilization efficiency, and environmental pollution caused by fossil fuel utilization, so it is urgent to accelerate the construction of a clean and low-carbon energy system.

[0004] Organic solid waste has the dual attributes of pollutants and resources. However, the direct combustion efficiency of organic solid waste is low, and the overall energy efficiency of the system is usually maintained below 35%. At the same time, a large amount of pollutants such as dioxins and acid gases are generated during the combustion process. Organic solid waste pyrolysis refers to the process of decomposing organic solid waste into pyrolysis oil, combustible gas and organic solid waste char through thermal chemical conversion under anaerobic or anoxic conditions. Organic solid waste pyrolysis technology can efficiently convert organic solid waste energy into various fuel substances or energy products, thereby reducing human dependence on fossil energy and alleviating environmental pollution caused by fossil energy consumption.

[0005] However, the traditional fluidized bed gasifier has poor adaptability to organic solid waste raw materials with high water content (>30%); the amount of tar generated is high, resulting in rising purification costs; a large amount of pollutants are also generated during pyrolysis; furthermore, the pyrolysis energy is single, and the combustible gas cannot be combined with by-product electricity and heat. SUMMARY

[0006] In order to overcome the above problems, the present application provides a hydrogen-electricity-heat cogeneration system and method for organic solid waste combustion and gasification.

[0007] To achieve the above technical purpose, the present application adopts the following technical solutions:

[0008] In a first aspect of the present application, a hydrogen-electricity-heat cogeneration system for organic solid waste combustion and gasification is provided, comprising:

[0009] A combustion furnace is used to burn high-calorific-value organic solid waste, and then to calcine limestone to generate CaO. The low calorific value of the high-calorific-value organic solid waste is ≥4500 kJ / kg, and the water content is ≤30%. The combustion furnace is connected with a first cyclone separator.

[0010] The first cyclone gas outlet is connected with a waste heat boiler, and the waste heat boiler is connected with an energy cascade utilization module; the energy cascade utilization module converts water vapor generated in the waste heat boiler into heat energy, electric energy and mechanical energy;

[0011] The first cyclone solid outlet is connected with a gasifier; the gasifier is used for gasifying low-calorific-value organic solid waste into hydrogen-rich gas under the catalysis of CaO; the low-calorific-value organic solid waste has a lower calorific value of <4500 kJ / kg or a water content of >30%.

[0012] The gasifier gas outlet is connected with a hydrogen purification module.

[0013] In one or more embodiments, the organic solid waste includes municipal solid waste, kitchen waste, food waste, agricultural and forestry waste, waste plastic, waste tire and municipal sludge.

[0014] In one or more embodiments, the combustion furnace is a circulating fluidized bed combustion furnace.

[0015] In one or more embodiments, the gasifier is a bubbling fluidized bed gasifier.

[0016] In one or more embodiments, the energy cascade utilization module includes a first water vapor pipeline, a second water vapor pipeline and a third water vapor pipeline; the temperature of water vapor in the first water vapor pipeline is higher than that in the second water vapor pipeline, and the temperature of water vapor in the second water vapor pipeline is higher than that in the third water vapor pipeline.

[0017] The first water vapor pipeline is connected with a steam turbine generator; water vapor drives the steam turbine generator to generate electricity to obtain electric energy.

[0018] The second water vapor pipeline is connected with a steam turbine; the steam turbine is connected with an air compressor in the hydrogen purification module; water vapor in the second water vapor pipeline drives the steam turbine blade to rotate, thereby driving the air compressor to compress hydrogen.

[0019] The third water vapor pipeline is respectively connected with a fourth water vapor pipeline and a fifth water vapor pipeline; the fourth water vapor pipeline is connected with the gasifier; the fifth water vapor pipeline discharges unused water vapor to obtain heat energy; water vapor in the fourth water vapor pipeline enters the gasifier to react with low-calorific-value organic solid waste to synthesize hydrogen.

[0020] In one or more embodiments, the gas outlet of the waste heat boiler is connected with a flue gas treatment module; the flue gas treatment module is used for desulfurization, denitrification, dechlorination, dioxin removal and dust removal of the gas generated in the combustion furnace.

[0021] Preferably, the flue gas treatment module comprises a first bag filter, a desulfurization tower, a second bag filter and an SCR denitration device connected in sequence.

[0022] Further preferably, a lime and activated carbon injection device is arranged between the first bag filter and the desulfurization tower.

[0023] In one or more embodiments, the solid outlet of the gasification furnace is connected to the combustion furnace through a return feeder; and the incompletely reacted furnace charge in the gasification furnace is transported to the combustion furnace through the return feeder to complete the calcium chemical looping cycle reaction and the semicoke combustion.

[0024] In one or more embodiments, the hydrogen purification and purification module comprises a second cyclone separator, a heat exchanger, a tar removal unit, a crude hydrogen storage tank and a pressure swing adsorption device connected in sequence; the tar removal unit comprises a washing tower and an electric tar catcher connected in sequence; and the pressure swing adsorption device comprises an air compressor; the hydrogen-rich gas in the gasification furnace is separated by the second cyclone separator and then enters the heat exchanger for cooling; the cooled gas enters the tar removal unit to remove tar, thereby completing the purification of hydrogen; the purified hydrogen enters the crude hydrogen storage tank and then enters the pressure swing adsorption device for purification; and the power of the air compressor in the pressure swing adsorption device is derived from the water vapor in the second water vapor pipeline, the water vapor in the second water vapor pipeline drives the turbine blades to rotate, thereby driving the air compressor to compress hydrogen.

[0025] In a second aspect of the present application, a hydrogen and heat cogeneration method for organic solid waste combustion and gasification is provided, comprising:

[0026] The high-calorific-value organic solid waste is mixed with limestone, the high-calorific-value organic solid waste is burned, and the limestone is calcined, thereby obtaining flue gas and furnace charge containing CaO;

[0027] The furnace charge containing CaO is mixed with low-calorific-value organic solid waste and water vapor is introduced, a hydrogen-rich gas is synthesized through gasification reaction; the hydrogen-rich gas is purified through pressure swing adsorption, thereby forming high-purity hydrogen;

[0028] The residual heat in the flue gas is absorbed by water to generate water vapor, the water vapor is arranged in three stages, i.e., high-temperature water vapor, medium-temperature water vapor and low-temperature water vapor, wherein the high-temperature water vapor is used for power generation; the medium-temperature water vapor drives the purified hydrogen-rich gas to be compressed; and the low-temperature water vapor participates in the gasification of the low-calorific-value organic solid waste.

[0029] In one or more embodiments, the low calorific value of the high-calorific-value organic solid waste is greater than or equal to 4500 kJ / kg and the water content is less than or equal to 30%.

[0030] In one or more embodiments, the low calorific value of the low-calorific-value organic solid waste is less than 4500 kJ / kg or the water content is greater than 30%.

[0031] In one or more embodiments, the high-temperature water vapor has a temperature of 400-450 DEG C, the medium-temperature water vapor has a temperature of 250-350 DEG C, and the low-temperature water vapor has a temperature of 150-200 DEG C.

[0032] The present application has the advantages of:

[0033] (1) In the present application, organic solid waste is divided into high-calorific-value organic solid waste and low-calorific-value organic solid waste based on calorific value and moisture content. The high-calorific-value organic solid waste is calcined with limestone, and the low-calorific-value organic solid waste is used for gasification. Not only does this effectively solve the industry problems of large temperature fluctuations (fluctuation range < ± 15 DEG C) and insufficient temperature (stably maintained at 850-950 DEG C) caused by traditional mixed feed, but also directly uses the moisture of low-calorific-value organic solid waste as a gasification reaction medium to participate in the water gas shift reaction (CO + H2O → CO2 + H2), significantly improving the hydrogen yield, while ensuring that the organic solid waste of different calorific values and moisture contents is fully quantized and digested, and solving the problem of unstable operation caused by the complex composition of organic solid waste.

[0034] (2) In terms of energy utilization, the traditional single power generation and single heat supply mode is innovated into a combined production mode of heat, electricity and mechanical energy by constructing a three-stage energy cascade utilization module. The waste heat boiler absorbs the waste heat in the flue gas of the combustion furnace to generate water vapor, which is arranged in three stages, i.e. high, medium and low temperature water vapor, of which the high-temperature water vapor is used for power generation; the medium-temperature water vapor drives the compression of the hydrogen-rich gas after purification; and the low-temperature water vapor participates in the gasification of low-calorific-value organic solid waste.

[0035] (3) In terms of pollution control, a "hydrogen production-pollution control" integrated technical solution is constructed: in the high-calorific-value organic solid waste combustion section, CaO efficiently captures SO2, HCl and Cl2 and other acidic gases, with a removal rate of more than 80%, significantly reducing the high-temperature corrosion risk of the superheater and improving the system thermal efficiency; and by efficiently removing Cl2, the generation of dioxins is inhibited from the source; in the low-calorific-value organic solid waste gasification section, CaO plays a dual role of catalytic cracking of tar and in-situ capture of CO2, improving the hydrogen yield and achieving carbon emission reduction. The combination of in-furnace deacidification and tail injection two-stage purification process constructs a complete near-zero emission system, providing key technical support for solving the "not-in-my-backyard" effect of organic solid waste treatment facilities, and also providing a replicable technical paradigm for "waste-free city" construction. BRIEF DESCRIPTION OF DRAWINGS

[0036] The accompanying drawings, which form a part of this specification, are included to provide a further understanding of the application and are incorporated herein by reference. The embodiments illustrated in the drawings and their descriptions are intended to explain the present application and are not intended to limit the present application.

[0037] Figure 1It is a structural schematic diagram of the hydrogen-electricity-heat cogeneration system for organic solid waste combustion and gasification in the application; wherein, 1-combustion furnace, 2-first cyclone separator, 3-waste heat boiler, 4-first bag-type dust collector, 5-lime and activated carbon injection device, 6-desulfurization tower, 7-second bag-type dust collector, 8-SCR denitration device, 9-gasification furnace, 10-second cyclone separator, 11-heat exchanger, 12-tar removal unit, 13-raw hydrogen storage tank, 14-pressure swing adsorption device, 15-feeding device, 16-energy cascade utilization module. DETAILED DESCRIPTION

[0038] It should be noted that the following detailed description is exemplary and is intended to provide further description of the application. Unless otherwise defined, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this application belongs.

[0039] It should be noted that the terms used herein are only for the purpose of describing specific embodiments and are not intended to limit exemplary embodiments according to the present application. As used herein, the singular form is intended to include the plural form unless the context clearly indicates otherwise, and it should also be understood that when the terms "comprise" and / or "include" are used in the specification, there is a reference to the presence of a feature, step, operation, device, component, and / or combinations thereof.

[0040] In order to enable those skilled in the art to more clearly understand the technical solutions of the present application, the technical solutions of the present application will be described in detail below with specific examples.

[0041] Example 1

[0042] Reference Figure 1 An organic solid waste combustion and gasification hydrogen-electricity-heat cogeneration system, comprising:

[0043] The combustion furnace 1 is used for burning high-calorific-value organic solid waste, and further calcining limestone to generate CaO, wherein the low calorific value of the high-calorific-value organic solid waste is ≥4500 kJ / kg and the water content is ≤30%; the combustion furnace 1 is connected with the first cyclone separator 2;

[0044] The gas outlet of the first cyclone separator 2 is connected with the waste heat boiler 3, and the waste heat boiler 3 is connected with the energy cascade utilization module 16; the energy cascade utilization module 16 converts the water vapor generated in the waste heat boiler 3 into heat energy, electric energy and mechanical energy;

[0045] The solid outlet of the first cyclone separator 2 is connected with the gasification furnace 9; the gasification furnace 9 is used for gasifying low-calorific-value organic solid waste into hydrogen-rich gas under the catalysis of CaO; the low calorific value of the low-calorific-value organic solid waste is <4500 kJ / kg and the water content is >30%;

[0046] The gas outlet of the gasification furnace 9 is connected with a hydrogen purification and refining module.

[0047] The organic solid waste includes municipal solid waste, kitchen waste, food waste, agricultural and forestry waste, waste plastic, waste tire, and municipal sludge.

[0048] The combustion furnace 1 is a circulating fluidized bed combustion furnace. The high-speed airflow in the circulating fluidized bed combustion furnace fully mixes the high-calorific-value organic solid waste and limestone to form a "fast fluidization" state. The fuel has a large contact area with oxygen, and the combustion reaction is more complete. The combustion efficiency is significantly higher than that of the traditional fixed bed combustion method. The flue gas and solids generated in the fluidized bed combustion furnace enter the first cyclone separator 2 under the action of the airflow.

[0049] The energy cascade utilization module 16 includes a first water vapor pipeline, a second water vapor pipeline, and a third water vapor pipeline. The temperature of the water vapor in the first steam pipeline is higher than that in the second water vapor pipeline, and the temperature of the water vapor in the second steam pipeline is higher than that in the third water vapor pipeline. Specifically, the water vapor parameters in the first steam pipeline are 6.4 MPa / 450 ℃, the water vapor parameters in the second steam pipeline are 1.2 MPa / 280 ℃, and the water vapor parameters in the third water vapor pipeline are 0.6 MPa / 160 ℃. The first water vapor pipeline is connected with a steam turbine generator. The water vapor drives the steam turbine generator to generate electricity to obtain electric energy. The second water vapor pipeline is connected with a steam turbine. The steam turbine is connected with an air compressor in the hydrogen purification and refining module. The water vapor in the second water vapor pipeline drives the steam turbine blades to rotate, thereby driving the air compressor to compress hydrogen. The third water vapor pipeline is connected with a fourth water vapor pipeline and a fifth water vapor pipeline, respectively. The fourth water vapor pipeline is connected with the gasification furnace 9. The fifth steam pipeline discharges the unused water vapor to obtain heat energy. The water vapor in the fourth water vapor pipeline enters the gasification furnace 9 to react with low-calorific-value organic solid waste to synthesize hydrogen. At the same time, the heat generated during the reaction can be used to maintain the high-temperature operation of the gasification furnace. Through the energy cascade utilization module 16, electric energy, mechanical energy, and heat energy are co-produced to realize efficient utilization of waste heat.

[0050] The gas outlet of the waste heat boiler 3 is connected with a flue gas purification module. The flue gas treatment module is used for desulfurization, denitrification, dechlorination, dioxin removal, and dust removal of the gas generated in the combustion furnace 1. The flue gas purification module includes a first bag-type dust collector 4, a desulfurization tower 6, a second bag-type dust collector 7, and an SCR denitration device 8 connected in sequence. A lime and activated carbon injection device 5 is arranged between the first bag-type dust collector 4 and the desulfurization tower 6.

[0051] The solid outlet of the gasification furnace 9 is connected with the combustion furnace 1 through a return feeder 15. The unreacted furnace charge in the gasification furnace 9 is transported to the combustion furnace 1 through the return feeder 15 to complete the calcium chemical looping cycle reaction and the semi-coke combustion.

[0052] The hydrogen gas purification module comprises a second cyclone separator 10, a heat exchanger 11, a tar removal unit 12, a crude hydrogen storage tank 13 and a pressure swing adsorption device 14 connected in sequence; the tar removal unit 12 comprises a washing tower and an electric coke capturing device connected in sequence, the heat exchanger 11 is connected with the washing tower, and the electric coke capturing device is connected with the crude hydrogen storage tank 13; the pressure swing adsorption device 14 comprises an air compressor; the hydrogen-rich gas in the gasification furnace 9 is separated by the second cyclone separator 10 and then enters the heat exchanger 11 to be cooled; the cooled gas enters the tar removal unit 12 to remove tar, thereby completing the purification of hydrogen gas; the purified hydrogen gas enters the crude hydrogen storage tank 13 and is finally purified in the pressure swing adsorption device 14; the power of the air compressor in the pressure swing adsorption device 14 is derived from the water vapor in the second water vapor pipeline, the water vapor in the second water vapor pipeline drives the turbine blades to rotate, thereby driving the air compressor to compress hydrogen gas.

[0053] The specific working process of the hydrogen and electricity cogeneration system of organic solid waste combustion and gasification is as follows:

[0054] The high-calorific-value organic solid waste is mixed with limestone in the combustion furnace 1, the high-calorific-value organic solid waste is burned, and the limestone is calcined, and the high-temperature flue gas (850 ℃ and above) and the CaO-containing furnace charge are obtained through the separation of the first cyclone separator 2.

[0055] The high-temperature flue gas enters the waste heat boiler 3 to heat the working water, and high, medium and low temperature water vapor is generated, the parameters of the high-temperature water vapor are 6.4 MPa / 450 ℃, the parameters of the medium-temperature water vapor are 1.2 MPa / 280 ℃, and the parameters of the low-temperature water vapor are 0.6 MPa / 160 ℃; the high-temperature water vapor enters the first water vapor pipeline and then enters the turbine generator to generate electricity to obtain electric energy; the medium-temperature flue gas enters the second water vapor pipeline to drive the turbine blades to rotate, thereby driving the air compressor in the pressure swing adsorption device 14 to compress hydrogen gas; part of the low-temperature water vapor is discharged from the system through the fourth steam pipeline to form a water vapor heat source, and the other part enters the gasification furnace 9 through the fifth water vapor pipeline to react with the low-calorific-value organic solid waste to synthesize hydrogen gas.

[0056] The flue gas in the waste heat boiler 3 after being cooled by heat absorption enters the flue gas purification module for desulfurization and denitrification, specifically, the flue gas after being cooled by heat absorption enters the first bag-type dust collector 4 for preliminary dust removal, and the desulfurization tower 6 for SO2, dioxin and heavy metal removal together with the lime and activated carbon sprayed by the lime and activated carbon spraying device 5; the flue gas enters the second bag-type dust collector 7 for secondary dust removal; and finally enters the SCR denitrification device 8 for denitrification, and the purified flue gas is discharged from the system;

[0057] In the gasifier 9, CaO in the furnace charge captures CO2 in situ as a carbon absorbent to promote hydrogen production from low-calorific-value organic solid waste and water vapor (including water vapor evaporated by itself and water vapor introduced through the fourth water vapor pipeline) gasification, to generate hydrogen-rich gas and semi-coke. The hydrogen-rich gas is separated by the second cyclone separator 10 and then enters the heat exchanger 11 for cooling. The cooled gas enters the scrubbing tower to remove tar, and then the purification of hydrogen is completed. The purified hydrogen enters the crude hydrogen storage tank 13, and then enters the pressure swing adsorption device 14 for purification. The power of the air compressor in the pressure swing adsorption device 14 is derived from the water vapor in the second water vapor pipeline. The water vapor in the second water vapor pipeline drives the turbine blades to rotate, and then drives the air compressor to compress the crude hydrogen gas.

[0058] The unreacted furnace charge in the gasifier 9 is transported to the combustion furnace 1 through the return feeder 15 to complete the calcium chemical chain cycle reaction and semi-coke combustion.

[0059] In the present application, the organic solid waste is divided into high-calorific-value organic solid waste and low-calorific-value organic solid waste based on calorific value and moisture content. The high-calorific-value organic solid waste is calcined with limestone, and the low-calorific-value organic solid waste is used for gasification. Not only does it effectively solve the industry problems of large temperature fluctuations (fluctuation range <±15℃) and insufficient temperature (stably maintained at 850-950℃) caused by traditional mixed feed, but also directly uses the moisture of low-calorific-value organic solid waste as a gasification reaction medium to participate in the water gas shift reaction (CO+H2O→CO2+H2), significantly improving the hydrogen production rate, while ensuring that all organic solid waste of different calorific values and moisture contents is fully digested, and completely solving the problem of unstable operation caused by complex components of organic solid waste.

[0060] In terms of energy utilization, the traditional single power generation and single heat supply mode is innovated into a combined production mode of thermal energy, electrical energy and mechanical energy by constructing a three-stage energy cascade utilization module. The waste heat boiler absorbs the waste heat in the combustion furnace flue gas to produce high, medium and low temperature water vapor, of which the high temperature water vapor is used for power generation, the medium temperature water vapor drives the compressed hydrogen-rich gas after purification, and the low temperature water vapor participates in the gasification of low-calorific-value organic solid waste.

[0061] In the present application, a calcium-based material internal circulation system is constructed, and through the recycling of CaO, biomass catalytic gasification and the controlled emission of pollutants are simultaneously achieved; in the high-calorific-value organic solid waste combustion section, CaO efficiently captures various acid gases such as SO2, HCl and Cl2, and the removal rate is stably above 80%, which significantly reduces the high-temperature corrosion risk of the superheater and improves the system thermal efficiency; more importantly, through the efficient removal of Cl2, the generation of dioxins is inhibited from the source; in the low-calorific-value organic solid waste gasification section, CaO plays a dual role of catalytic cracking of tar and in-situ capture of CO2, which improves the hydrogen yield and achieves carbon emission reduction. The combination of in-furnace deacidification and tail injection two-stage purification process constructs a complete near-zero emission system, which provides key technical support for solving the "not-in-my-backyard" effect of organic solid waste treatment facilities, and also provides a replicable technical paradigm for "waste-free city" construction.

[0062] In the present application, CaO generated by calcination in the combustion furnace is used to remove SO2, HCl, chlorine, dioxins and nitrogen oxides generated in the incineration of organic solid waste, so that the SO2 content in the finally discharged flue gas is less than 10 mg / Nm 3 , the chlorine ion concentration is less than or equal to 10 mg / Nm 3 , the dioxin is less than or equal to 0.015 ng TEQ / m 3 , and the nitrogen oxides are less than 30 mg / Nm 3 .

[0063] In the present embodiment, the calorific values of high-calorific-value organic solid waste and low-calorific-value organic solid waste are monitored in real time by a calorific value detection device, and compared with a preset threshold value, and the feeding rate of high-calorific-value organic solid waste and low-calorific-value organic solid waste, the primary air volume, and the flue gas recirculation rate are dynamically adjusted by a PID algorithm to maintain the furnace temperature fluctuation within ±10 ℃ and the combustion furnace fluidization wind speed within 4.5-6.5 m / s. The intelligent control method based on online calorific value detection can monitor the calorific value and moisture content of organic solid waste in real time, automatically and in real time control the primary and secondary air and the flue gas recirculation rate, maintain the combustion furnace temperature and flue gas flow rate stable, maintain the hydrogen production amount and composition stable, and enhance the system operation stability.

[0064] In the combustion furnace 1, CaCO3 in high-calorific-value organic solid waste is calcined to generate CaO, and the temperature is 850-950 ℃; in the gasification furnace 9, low-calorific-value organic solid waste is gasified under the catalysis of CaO, and the temperature is 650-720 ℃; the circulation rate of CaCO3 and CaO furnace charge is 0.5-1.2 kg / (m 2 ·s), and the mass ratio of CaO to CaCO3 in the furnace charge is 6:4-7:3, and the particle size of the calcium-based furnace charge is 100-300 μm.

[0065] According to the hydrogen storage amount in the crude hydrogen storage tank 13 and the power grid demand priority, the steam energy is dynamically allocated, when the hydrogen storage amount is lower than the safety threshold, the medium-pressure steam is preferentially used to drive the pressure swing adsorption air compressor, and when the power grid peak shaving demand exceeds the set value, the high-pressure steam power generation proportion is increased.

[0066] Embodiment 2

[0067] A hydrogen and electricity cogeneration method for organic solid waste combustion and gasification, comprising:

[0068] Mixing high-calorific-value organic solid waste with limestone, burning the high-calorific-value organic solid waste, and further calcining the limestone to obtain flue gas and a CaO-containing charge;

[0069] Mixing the CaO-containing charge with low-calorific-value organic solid waste and passing steam into the mixture, and synthesizing hydrogen-rich gas through gasification reaction; after purification, the hydrogen-rich gas is purified by pressure swing adsorption to form high-purity hydrogen gas;

[0070] The residual heat in the flue gas is absorbed by water to generate steam, and the steam is arranged in three stages, wherein the high-temperature steam is used for power generation; the medium-temperature steam drives the compression of the purified hydrogen-rich gas; and the low-temperature steam participates in the gasification of the low-calorific-value organic solid waste.

[0071] The low calorific value of the high-calorific-value organic solid waste is ≥4500 kJ / kg and the water content is ≤30%.

[0072] The low calorific value of the low-calorific-value organic solid waste is <4500 kJ / kg and the water content is >30%.

[0073] The parameters of the high-temperature steam are 6.4 MPa / 450 DEG C, the parameters of the medium-temperature steam are 1.2 MPa / 280 DEG C, and the parameters of the low-temperature steam are 0.6 MPa / 160 DEG C.

[0074] The above only describes the preferred embodiments of the present application and is not used to limit the present application. For those skilled in the art, the present application can have various modifications and changes. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present application shall be included in the protection scope of the present application.

Claims

1. A hydrogen and electricity cogeneration system for organic solid waste combustion and gasification, characterized in that, include: A combustion furnace, which is connected to a first cyclone separator; The gas outlet of the first cyclone separator is connected to a waste heat boiler, which is connected to an energy cascade utilization module. The energy cascade utilization module converts the steam generated in the waste heat boiler into thermal energy, electrical energy, and mechanical energy; The energy cascade utilization module includes a first steam pipe, a second steam pipe, and a third steam pipe; wherein, the temperature of the steam in the first steam pipe is higher than that in the second steam pipe, and the temperature of the steam in the second steam pipe is higher than that in the third steam pipe. The first steam pipe is connected to a steam turbine generator; the steam drives the steam turbine generator to generate electricity; the second steam pipe is connected to a steam turbine; the steam turbine is connected to an air compressor in the hydrogen purification module; the steam in the second steam pipe drives the turbine blades to rotate, thereby driving the air compressor to compress hydrogen; the third steam pipe is connected to the fourth and fifth steam pipes respectively; the fourth steam pipe is connected to a gasifier; the fifth steam pipe discharges unused steam to obtain heat energy; The solid outlet of the first cyclone separator is connected to the gasifier; The gas outlet of the gasifier is connected to a hydrogen purification and upgrading module.

2. The organic solid waste combustion-cogeneration system of claim 1, wherein, The organic solid waste includes: municipal solid waste, kitchen waste, food waste, agricultural and forestry waste, waste plastics, waste tires, and municipal sludge; Alternatively, the combustion furnace is a circulating fluidized bed combustion furnace; Alternatively, the gasifier may be a bubbling fluidized bed gasifier.

3. The organic solid waste combustion-cogeneration system of claim 1, wherein, The gas outlet of the waste heat boiler is connected to the flue gas treatment module; the flue gas treatment module is used for desulfurization, denitrification, dechlorination, dioxin removal and dust removal of the gas generated in the combustion furnace.

4. The organic solid waste combustion-cogeneration system of claim 3, wherein The flue gas treatment module includes a first bag filter, a desulfurization tower, a second bag filter, and an SCR denitrification device connected in sequence.

5. The organic solid waste combustion-cogasification based hydrogen cogeneration system of claim 4, wherein, A quicklime and activated carbon injection device is installed between the first bag filter and the desulfurization tower.

6. The organic solid waste combustion-cogeneration system of hydrogen and electricity of claim 1, wherein The solid outlet of the gasifier is connected to the combustion furnace via a return feeder.

7. The organic solid waste combustion-cogeneration system of hydrogen and electricity of claim 1, wherein The hydrogen purification module includes a second cyclone separator, a heat exchanger, a tar removal unit, a crude hydrogen storage tank, and a pressure swing adsorption device connected in sequence; the tar removal unit includes a scrubbing tower and an electrostatic precipitator connected in sequence.

8. A method for hydrogen-electricity-heat cogeneration from organic solid waste combustion and gasification using the hydrogen-electricity-heat cogeneration system for organic solid waste combustion and gasification according to any one of claims 1 to 7, characterized in that, include: High-calorific-value organic solid waste is mixed with limestone, the high-calorific-value organic solid waste is burned, and then the limestone is calcined to obtain flue gas and furnace charge containing CaO. The furnace charge containing CaO is mixed with low-calorific-value organic solid waste and steam is introduced to gasify and synthesize hydrogen-rich gas. After purification, the hydrogen-rich gas is further purified by pressure swing adsorption to form high-purity hydrogen. The residual heat in the flue gas is absorbed by water to generate steam. The steam is arranged in three stages: high-temperature steam is used for power generation; medium-temperature steam drives the compression of purified hydrogen-rich gas; and low-temperature steam participates in the gasification of low-calorific-value organic solid waste.

9. The method of claim 8, wherein the organic solid waste combustion- syngas co- gasification is characterized by, The high-calorific-value organic solid waste has a lower heating value ≥ 4500 kJ / kg and a moisture content ≤ 30%; Alternatively, the lower heating value of the low-calorific-value organic solid waste is <4500 kJ / kg or the moisture content is >30%.

10. The method of claim 8, wherein the organic solid waste combustion- syngas co- gasification is characterized by, The high-temperature water vapor has a temperature of 400-450 ℃, the medium-temperature water vapor has a temperature of 250-350 ℃, and the low-temperature water vapor has a temperature of 150-200 ℃. The high-temperature water vapor has a temperature of 400-450 ℃, the medium-temperature water vapor has a temperature of 250-350 ℃, and the low-temperature water

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