A reaction regulation method and system

Abstract

The present disclosure provides a reaction regulation method, comprising: introducing a carbon-based raw material, a gasification agent, and an auxiliary gas into a gasification unit to generate carbon-containing gasification ash; introducing the carbon-containing gasification ash and an oxidizing agent into a hearth of a boiler unit, and introducing water at a predetermined temperature into a heat exchange tube bundle of the boiler unit, and using heat generated by a combustion reaction to exchange heat with the water at the predetermined temperature in the heat exchange tube bundle to generate first steam; introducing the first steam generated by the boiler unit into a power generation unit; obtaining, in a current time period, an actual effective gas amount in dust-containing product gas of the gasification unit, an actual power generation amount of the power generation unit, user effective gas demand information, and user power generation demand information; and regulating the gasification reaction in the gasification unit based on predetermined regulation parameters according to the actual effective gas amount, the actual power generation amount, the effective gas demand information, and the power generation demand information.

Description

Technical Field

[0001] This invention relates to the field of coal gasification technology, specifically to a reaction control method and system. Background Technology

[0002] Directly burning coal ignores its raw material properties, resulting in a significant waste of its high-value hydrogen-rich components and impacting the overall utilization level and efficiency of coal. However, if only the raw material properties of coal are considered, direct coal gasification presents several challenges. First, to ensure a high carbon conversion rate, existing technologies impose high requirements on coal quality and reaction conditions, leading to high conversion costs. Second, the fly ash and bottom ash generated during gasification require separate disposal as solid waste. Furthermore, coal gasification and subsequent chemical synthesis processes require substantial amounts of steam and electricity, which still originate directly or indirectly from coal combustion. Summary of the Invention

[0003] In view of the above problems, the present invention provides a reaction regulation method and system.

[0004] One aspect of the present invention provides a reaction regulation method, comprising:

[0005] Carbon-based raw materials, gasifying agents, and auxiliary gases are introduced into the gasification unit so that the carbon-based raw materials, gasifying agents, and auxiliary gases undergo a gasification reaction in the gasification unit to obtain dust-containing product gas at a first temperature, while generating carbon-containing gasification ash. The dust-containing product gas includes effective gases for the gas synthesis process.

[0006] Carbon-containing gasification ash and oxidant are introduced into the furnace of the boiler unit, and water at a predetermined temperature is introduced into the heat exchange tube bundle of the boiler unit so that the carbon-containing gasification ash and oxidant can undergo a combustion reaction in the furnace, and the heat generated by the combustion reaction is used to exchange heat with the water at a predetermined temperature in the heat exchange tube bundle to generate the first steam.

[0007] The first steam generated by the boiler unit is fed into the power generation unit so that the heat energy of the first steam can be converted into electrical energy through the power generation unit;

[0008] Obtain the actual effective gas volume in the dust-laden product gas of the gasification unit, the actual power generation of the power generation unit, the effective gas volume demand of the user, and the power generation demand of the user in the current time period.

[0009] Based on the actual effective gas volume, actual power generation, effective gas volume demand information, and power generation demand information, the gasification reaction in the gasification unit is regulated according to predetermined adjustment parameters.

[0010] According to embodiments of this disclosure, the auxiliary gas includes water vapor and / or carbon dioxide;

[0011] The dust-laden product gas includes at least carbon monoxide, hydrogen, and carbon dioxide, wherein the effective gases in the dust-laden product gas include at least carbon monoxide and hydrogen;

[0012] The vaporizing agent includes oxygen components and non-oxygen components;

[0013] The predetermined adjustment parameters include at least one of the following: the amount of carbon-based feedstock, the equivalence ratio of the gasification unit, the component ratio of oxygen and non-oxygen components in the gasifying agent, the ratio of water vapor to carbon-based feedstock, the ratio of carbon dioxide to carbon-based feedstock, the total amount of gasifying agent, and the particle size of the carbon-based feedstock.

[0014] According to embodiments of this disclosure, regulating the gasification reaction in the gasification unit based on predetermined adjustment parameters, according to the actual effective gas quantity, actual power generation, effective gas quantity demand information, and power generation demand information, includes:

[0015] Based on the actual effective gas quantity, actual power generation, effective gas quantity demand information, and power generation demand information, if the control direction is determined to be either increasing the effective gas quantity in the dust-containing product gas or decreasing the power generation, the following operations are performed: maintaining the carbon-based raw material feed rate unchanged, maintaining the component ratio of the gasifying agent unchanged, maintaining the ratio of water vapor to carbon-based raw material unchanged, maintaining the ratio of carbon dioxide to carbon-based raw material unchanged, and increasing the total feed rate of the gasifying agent to reduce the equivalence ratio of the gasification unit.

[0016] Based on the actual effective gas quantity, actual power generation, effective gas quantity demand information, and power generation demand information, if the control direction is determined to be reducing the effective gas quantity in the dust-containing product gas or increasing power generation, the following operations are performed: maintaining the carbon-based raw material feed rate unchanged, maintaining the component ratio of the gasifying agent unchanged, maintaining the ratio of water vapor to carbon-based raw material unchanged, maintaining the ratio of carbon dioxide to carbon-based raw material unchanged, and reducing the total feed rate of the gasifying agent to increase the equivalence ratio of the gasification unit.

[0017] According to embodiments of this disclosure, the reaction regulation method further includes:

[0018] The gasification reaction temperature of the gasification unit is monitored, and a safety warning command is generated when the gasification reaction temperature is greater than or equal to a first temperature threshold. The first temperature threshold is calculated based on the softening temperature of the carbon-containing gasification ash.

[0019] The rate of change of calorific value of carbon-containing gasification ash is calculated as a function of gasification reaction temperature, and energy transfer analysis results are generated based on the rate of change of calorific value. The energy transfer analysis results are used to characterize whether more energy in the carbon-based feedstock is transferred to the product gas (coal gas) or more energy is transferred to steam / electricity products.

[0020] According to embodiments of this disclosure, regulating the gasification reaction in the gasification unit based on predetermined adjustment parameters, according to the actual effective gas quantity, actual power generation, effective gas quantity demand information, and power generation demand information, includes:

[0021] Based on the actual effective gas volume, actual power generation, effective gas volume demand information, and power generation demand information, if the control direction is determined to be to increase the effective gas volume in the dust-containing product gas, the following operations are performed: maintaining the equivalence ratio of the gasification unit unchanged, maintaining the component ratio of the gasifying agent unchanged, maintaining the ratio of water vapor to carbon-based raw materials unchanged, maintaining the ratio of carbon dioxide to carbon-based raw materials unchanged, increasing the feed amount of carbon-based raw materials, and increasing the total feed amount of the gasifying agent, so as to increase the gasification load of the gasification unit.

[0022] Based on the actual effective gas volume, actual power generation, effective gas volume demand information, and power generation demand information, if the control direction is determined to be to reduce the effective gas volume in the dust-containing product gas, the following operations are performed: maintaining the equivalence ratio of the gasification unit unchanged, maintaining the component ratio of the gasifying agent unchanged, maintaining the ratio of water vapor to carbon-based raw materials unchanged, maintaining the ratio of carbon dioxide to carbon-based raw materials unchanged, reducing the feed amount of carbon-based raw materials, and reducing the total feed amount of the gasifying agent, so as to reduce the gasification load of the gasification unit.

[0023] According to embodiments of this disclosure, the reaction regulation method further includes:

[0024] Monitor the gasification reaction temperature and gasification load of the gasification unit;

[0025] When the gasification reaction temperature is greater than or equal to the second temperature threshold and the gasification load of the gasification unit is greater than or equal to the predetermined load threshold, a first energy transfer analysis result is generated, wherein the first energy transfer analysis result is used to characterize that more energy in the carbon-based feedstock is transferred to the product gas;

[0026] When the gasification reaction temperature is less than the second temperature threshold and the gasification load of the gasification unit is less than the predetermined load threshold, a second energy transfer analysis result is generated, wherein the second energy transfer analysis result is used to characterize that more energy in the carbon-based feedstock is transferred to the steam / electric products.

[0027] According to embodiments of this disclosure, regulating the gasification reaction in the gasification unit based on predetermined adjustment parameters, according to the actual effective gas quantity, actual power generation, effective gas quantity demand information, and power generation demand information, includes:

[0028] Based on the actual effective gas quantity, actual power generation, effective gas quantity demand information, and power generation demand information, if the control direction is determined to be either increasing the effective gas quantity in the dust-containing product gas or decreasing the power generation, the following operations are performed: maintaining the equivalence ratio of the gasification unit unchanged, maintaining the feed amount of carbon-based raw materials unchanged, maintaining the ratio of water vapor to carbon-based raw materials unchanged, maintaining the ratio of carbon dioxide to carbon-based raw materials unchanged, increasing the component proportion of oxygen in the gasifying agent, and decreasing the total feed amount of the gasifying agent.

[0029] Based on the actual effective gas quantity, actual power generation, effective gas quantity demand information, and power generation demand information, if the control direction is determined to be reducing the effective gas quantity in the dust-containing product gas or increasing power generation, the following operations are performed: maintaining the equivalence ratio of the gasification unit unchanged, maintaining the feed amount of carbon-based raw materials unchanged, maintaining the ratio of water vapor to carbon-based raw materials unchanged, maintaining the ratio of carbon dioxide to carbon-based raw materials unchanged, reducing the component proportion of oxygen in the gasifying agent, and increasing the total feed amount of the gasifying agent.

[0030] According to embodiments of this disclosure, regulating the gasification reaction in the gasification unit based on predetermined adjustment parameters, according to the actual effective gas quantity, actual power generation, effective gas quantity demand information, and power generation demand information, includes:

[0031] Based on the actual effective gas volume, actual power generation, effective gas volume demand information, and power generation demand information, if the control direction is determined to be either reducing the effective gas volume in the dust-laden product gas or increasing power generation, the following operations shall be performed:

[0032] The equivalence ratio of the gasification unit remains constant, the amount of carbon-based feedstock remains constant, the component ratio of the gasifying agent remains constant, the ratio of steam to carbon-based feedstock remains constant, the ratio of carbon dioxide to carbon-based feedstock remains constant, and the total amount of gasifying agent is kept constant.

[0033] The current value of the particle size of the carbon-based raw material is measured;

[0034] If the current value of the particle size of the carbon-based feedstock is less than the first reference value, the particle size of the carbon-based feedstock introduced into the gasification unit is reduced, wherein the first reference value is calculated based on the median particle size of fly ash at the outlet of the cyclone separator of the gasification unit.

[0035] If the current value of the particle size of the carbon-based feedstock is greater than the second reference value, the particle size of the carbon-based feedstock introduced into the gasification unit is increased. The second reference value is calculated based on the median particle size of fly ash at the outlet of the cyclone separator of the gasification unit and is greater than the first reference value.

[0036] According to embodiments of this disclosure, regulating the gasification reaction in the gasification unit based on predetermined adjustment parameters, according to the actual effective gas quantity, actual power generation, effective gas quantity demand information, and power generation demand information, includes:

[0037] Based on the actual effective gas quantity, actual power generation, effective gas quantity demand information, and power generation demand information, if the control direction is determined to be to increase the effective gas quantity in the dust-containing product gas or to decrease the power generation, the following operations are performed: maintain the carbon-based raw material feed rate unchanged, maintain the oxygen component ratio in the gasifying agent unchanged, maintain the carbon dioxide to carbon-based raw material ratio unchanged, reduce the equivalence ratio of the gasification unit, increase the water vapor to carbon-based raw material ratio, and maintain the gasification temperature unchanged.

[0038] Based on the actual effective gas volume, actual power generation, effective gas volume demand information, and power generation demand information, if the control direction is determined to be either reducing the effective gas volume in the dust-containing product gas or increasing power generation, the following operations are performed: maintaining the feed amount of carbon-based raw materials unchanged, maintaining the proportion of oxygen components in the gasifying agent unchanged, maintaining the ratio of carbon dioxide to carbon-based raw materials unchanged, increasing the equivalence ratio of the gasification unit, decreasing the ratio of water vapor to carbon-based raw materials, and maintaining the gasification temperature unchanged.

[0039] According to embodiments of this disclosure, regulating the gasification reaction in the gasification unit based on predetermined adjustment parameters, according to the actual effective gas quantity, actual power generation, effective gas quantity demand information, and power generation demand information, includes:

[0040] Based on the actual effective gas quantity, actual power generation, effective gas quantity demand information, and power generation demand information, if the control direction is determined to be to increase the effective gas quantity in the dust-containing product gas or to decrease the power generation, the following operations are performed: maintain the carbon-based raw material feed rate unchanged, maintain the oxygen component ratio in the gasifying agent unchanged, maintain the ratio of water vapor to carbon-based raw material unchanged, reduce the equivalence ratio of the gasification unit, increase the ratio of carbon dioxide to carbon-based raw material, and maintain the gasification temperature unchanged.

[0041] Based on the actual effective gas volume, actual power generation, effective gas volume demand information, and power generation demand information, if the control direction is determined to be either reducing the effective gas volume in the dust-containing product gas or increasing power generation, the following operations are performed: maintaining the carbon-based raw material feed rate constant, maintaining the oxygen component ratio in the gasifying agent constant, maintaining the ratio of water vapor to carbon-based raw material constant, increasing the equivalence ratio of the gasification unit, decreasing the ratio of carbon dioxide to carbon-based raw material, and maintaining the gasification temperature constant.

[0042] According to embodiments of this disclosure, the reaction regulation method further includes:

[0043] Dust-laden product gas at a first temperature and water at a predetermined temperature are introduced into the waste heat recovery unit so that the dust-laden product gas at the first temperature and the water at the predetermined temperature exchange heat in the waste heat recovery unit to obtain dust-laden product gas at a second temperature and second steam.

[0044] The second steam is introduced into the power generation unit so that the heat energy of the second steam and the first steam can be converted into electrical energy through the power generation unit;

[0045] The dust-laden product gas at the second temperature is passed into the dust removal unit for gas-solid separation to obtain dust-free product gas and carbon-containing fly ash.

[0046] Carbonaceous fly ash is introduced into the furnace of the boiler unit so that the carbonaceous fly ash and carbonaceous gasification ash are burned together as fuel in the furnace.

[0047] The dust-free product gas is passed into the conversion unit for gas conversion to obtain sulfur-containing product gas. The conversion reaction includes: carbon monoxide in the dust-free product gas reacts with water vapor passed into the conversion unit to produce carbon dioxide and hydrogen.

[0048] The sulfur-containing product gas is passed into the first desulfurization unit for sulfide recovery, resulting in carbon-containing product gas and sulfur product.

[0049] Carbon-containing product gas is passed into a decarbonization unit to remove carbon dioxide, thereby obtaining the target product gas. The removed carbon dioxide can be used for gasification in the gasification unit.

[0050] The flue gas produced by the combustion reaction in the boiler unit is passed into the second desulfurization unit for desulfurization.

[0051] Another aspect of the present invention provides a reaction control system, comprising:

[0052] The gasification unit is used to gasify carbon-based raw materials, gasifying agents, and auxiliary gases to obtain dust-containing product gas at a first temperature, while generating carbon-containing gasification ash. The dust-containing product gas includes effective gases used in the gas synthesis process.

[0053] A boiler unit is used for the combustion reaction of carbon-containing gasification ash and oxidant in the furnace of the boiler unit, and the heat generated by the combustion reaction is exchanged with water at a predetermined temperature in the heat exchange tube bundle of the boiler unit to generate first steam.

[0054] A power generation unit is used to convert the thermal energy of the first steam into electrical energy.

[0055] The control unit is used to acquire, within the current time period, the actual effective gas quantity in the dust-laden product gas of the gasification unit, the actual power generation of the power generation unit, the effective gas quantity demand information of the user, and the power generation demand information of the user. Based on the actual effective gas quantity, actual power generation, effective gas quantity demand information, and power generation demand information, it controls the gasification reaction in the gasification unit according to predetermined adjustment parameters.

[0056] According to embodiments of this disclosure, the reaction control system further includes:

[0057] The waste heat recovery unit is used to exchange heat between the dust-laden product gas at a first temperature and water at a predetermined temperature to obtain the dust-laden product gas at a second temperature and the second steam, wherein the second steam is fed into the power generation unit.

[0058] The dust removal unit is used to perform gas-solid separation on the dust-laden product gas at the second temperature to obtain dust-free product gas and carbon-containing fly ash, wherein the carbon-containing fly ash is introduced into the furnace of the boiler unit.

[0059] The shift unit is used to convert dust-free product gas into sulfur-containing product gas through a shift reaction. The shift reaction includes: carbon monoxide in the dust-free product gas reacts with water vapor introduced into the shift unit to produce carbon dioxide and hydrogen.

[0060] The first desulfurization unit is used to recover sulfides from sulfur-containing product gas to obtain carbon-containing product gas and sulfur products.

[0061] The decarbonization unit is used to remove carbon dioxide from carbon-containing product gas to obtain the target product gas.

[0062] The second desulfurization unit is used to desulfurize the flue gas generated by the combustion reaction in the boiler unit.

[0063] According to embodiments of this disclosure, during the gasification process of carbon-based raw materials, by adjusting the content and proportions of the carbon-based raw materials, gasifying agent, and auxiliary gas, the direction of the gasification products towards gaseous or electrical products can be indirectly controlled, thereby meeting users' electricity or gas consumption needs while achieving energy conservation. Furthermore, by adjusting predetermined parameters (such as adjusting the amount of auxiliary gas entering or the proportions of its components), the gasification products can be further controlled to be produced towards effective gases (such as carbon monoxide and hydrogen) or towards steam / electricity. This method takes into account both the raw material and fuel properties of coal, realizing the conversion of matter and energy in the system. While optimizing the matching of gas and electricity production, it maximizes the conversion process between raw materials and products, achieving maximum economic and social benefits. Attached Figure Description

[0064] Figure 1A schematic diagram of the reaction control system according to an embodiment of the present disclosure is shown.

[0065] Figure 2 A schematic diagram of a reaction control system according to another embodiment of the present disclosure is shown.

[0066] Figure 3 A schematic diagram of a reaction control system according to yet another embodiment of the present disclosure is shown.

[0067] Figure 4 A flowchart illustrating a reaction regulation method according to an embodiment of the present disclosure is shown schematically.

[0068] Figure 5 A flowchart illustrating another embodiment of the reaction regulation method of this disclosure is shown schematically. Detailed Implementation

[0069] To make the objectives, technical solutions, and advantages of the present invention clearer, the present invention will be further described in detail below with reference to specific embodiments and accompanying drawings.

[0070] The embodiments of the present disclosure will now be described with reference to the accompanying drawings. However, it should be understood that these descriptions are exemplary only and are not intended to limit the scope of the disclosure. In the following detailed description, numerous specific details are set forth to provide a thorough understanding of the embodiments of the present disclosure for ease of explanation. However, it will be apparent that one or more embodiments may be practiced without these specific details. Furthermore, descriptions of well-known structures and techniques are omitted in the following description to avoid unnecessarily obscuring the concepts of the present disclosure.

[0071] The terminology used herein is for the purpose of describing particular embodiments only and is not intended to limit this disclosure. The terms “comprising,” “including,” etc., as used herein indicate the presence of features, steps, operations, and / or components, but do not exclude the presence or addition of one or more other features, steps, operations, or components.

[0072] All terms used herein (including technical and scientific terms) have the meanings commonly understood by those skilled in the art, unless otherwise defined. It should be noted that the terms used herein are to be interpreted in a manner consistent with the context of this specification, and not in an idealized or overly rigid way.

[0073] When using expressions such as "at least one of A, B, and C," the expression should generally be interpreted in accordance with the meaning commonly understood by a person skilled in the art (e.g., "a system having at least one of A, B, and C" should include, but is not limited to, systems having A alone, having B alone, having C alone, having A and B, having A and C, having B and C, and / or having A, B, and C, etc.). When using expressions such as "at least one of A, B, or C," the expression should generally be interpreted in accordance with the meaning commonly understood by a person skilled in the art (e.g., "a system having at least one of A, B, or C" should include, but is not limited to, systems having A alone, having B alone, having C alone, having A and B, having A and C, having B and C, and / or having A, B, and C, etc.).

[0074] In one aspect, the present invention provides a reaction control system.

[0075] Figure 1 A schematic diagram of the reaction control system according to an embodiment of the present disclosure is shown.

[0076] like Figure 1 As shown, the reaction control system includes at least a gasification unit 110, a boiler unit 120, and a power generation unit 130.

[0077] Gasification unit 110 is used to perform a gasification reaction of carbon-based raw materials, gasifying agent, and auxiliary gas in gasification unit 110 to obtain dust-containing product gas at a first temperature (high-temperature dust-containing product gas, for example, 700-1100℃), while simultaneously generating carbon-containing gasification ash. The dust-containing product gas includes effective gases used in the gas synthesis process. Gasification unit 110 is provided with a carbon-based raw material inlet, a gasifying agent inlet, an auxiliary gas inlet, a dust-containing product gas outlet, and a carbon-containing gasification ash outlet. The auxiliary gas includes water vapor and / or carbon dioxide; the dust-containing product gas includes at least carbon monoxide, hydrogen, and carbon dioxide, and the effective gases in the dust-containing product gas include at least carbon monoxide and hydrogen; the gasifying agent includes oxygen and non-oxygen components.

[0078] Boiler unit 120 is used for the combustion reaction of carbonaceous gasification ash and oxidant in the furnace of boiler unit 120. The heat generated by the combustion reaction is exchanged with water at a predetermined temperature (e.g., 0-100°C) in the heat exchange tube bundle of boiler unit 120 to generate first steam. Boiler unit 120 is provided with a carbonaceous gasification ash inlet, a first cold water inlet, an oxidant inlet (not shown in the figure), a carbonaceous fly ash inlet (not shown in the figure), a denitrification agent inlet (not shown in the figure), a first steam outlet, and a flue gas outlet. The carbonaceous gasification ash inlet of boiler unit 120 is connected to the carbonaceous gasification ash outlet of gasification unit 110; the carbonaceous fly ash inlet of boiler unit 120 is connected to the carbonaceous fly ash outlet of dust removal unit 150; and the first steam outlet of boiler unit 120 is connected to the first steam inlet of power generation unit 130.

[0079] Boiler unit 120 can be a circulating fluidized bed boiler. By matching the density, particle size, carbon content, and other parameters of the residue and fly ash from gasification unit 110, a normal circulation loop is established, thereby achieving stable combustion of pure gasified fly ash within the boiler. Furthermore, by using bottom ash with a particle size of 0 mm to 6 mm from gasification unit 110 as circulating bed material and ash with a particle size less than 0.2 mm as the main fuel, stable combustion of pure gasified ash within the circulating fluidized bed boiler can be achieved.

[0080] The power generation unit 130 is used to convert the thermal energy of the first steam into electrical energy. The power generation unit 130 is provided with a first steam inlet. The first steam inlet of the power generation unit 130 is connected to the first steam outlet of the boiler unit 120. The exhaust gas generated after the steam performs work can enter the gasification unit 110 through the gasifying agent inlet, participating in the gasification reaction as a gasifying agent (not shown in the figure). The power generation unit 130 can also convert the thermal energy of the second steam into electrical energy. The power generation unit 130 can also be provided with a second steam inlet (not shown in the figure), which is connected to the second steam outlet of the waste heat recovery unit 140 (not shown in the figure).

[0081] According to embodiments of this disclosure, the reaction control system further includes a control unit (not shown in the figure), used to acquire, during the current time period, the actual effective gas quantity in the dust-containing product gas of the gasification unit 110, the actual power generation of the power generation unit 130, the effective gas quantity demand information of the user, and the power generation demand information of the user, and to control the gasification reaction in the gasification unit 110 based on predetermined control parameters according to the actual effective gas quantity, the actual power generation of the power generation unit 130, the effective gas quantity demand information of the user, and the power generation demand information of the user.

[0082] Figure 2 A schematic diagram of a reaction control system according to another embodiment of the present disclosure is shown.

[0083] like Figure 2 As shown, the reaction control system also includes a waste heat recovery unit 140, a dust removal unit 150, a conversion unit 160, a first desulfurization unit 170, a decarbonization unit 180, and a second desulfurization unit 190. Among these,

[0084] The waste heat recovery unit 140 is used to exchange heat between dust-laden product gas at a first temperature (high-temperature dust-laden product gas, e.g., 700–1100°C) and water at a predetermined temperature (e.g., 0–100°C) to obtain dust-laden product gas at a second temperature (low-temperature dust-laden product gas, e.g., 100–250°C) and second steam. The second steam is then introduced into the power generation unit 130. The waste heat recovery unit 140 is equipped with a dust-laden product gas inlet, a second cold water inlet, a dust-laden product gas outlet, and a second steam outlet. The dust-laden product gas inlet of the waste heat recovery unit 140 is connected to the dust-laden product gas outlet of the gasification unit 110. Furthermore, the second steam generated by the waste heat recovery unit 140 can first enter the boiler unit 120 for further superheating to improve steam quality, converting it into first steam before entering the power generation unit 130 to generate electricity.

[0085] The dust removal unit 150 is used to perform gas-solid separation on the dust-laden product gas at a second temperature (low-temperature dust-laden product gas, for example, 100-250°C) to obtain dust-free product gas and carbon-containing fly ash, wherein the carbon-containing fly ash is introduced into the furnace of the boiler unit 120; wherein the dust removal unit 150 is provided with a dust-laden product gas inlet, a dust-free product gas outlet and a carbon-containing fly ash outlet, and the dust-laden product gas inlet of the dust removal unit 150 is connected to the dust-laden product gas outlet of the waste heat recovery unit 140.

[0086] The conversion unit 160 is used to perform a conversion reaction on the dust-free product gas to obtain a sulfur-containing product gas. The conversion reaction includes the reaction of carbon monoxide in the dust-free product gas with water vapor introduced into the conversion unit to generate carbon dioxide and hydrogen (not shown in the figure). The conversion unit 160 is provided with a dust-free product gas inlet, a sulfur-containing product gas outlet, and a second steam inlet. The dust-free product gas inlet of the conversion unit 160 is connected to the dust-free product gas outlet of the dust removal unit 150.

[0087] The first desulfurization unit 170 is used to recover sulfides from sulfur-containing product gas to obtain carbon-containing product gas and sulfur product. The first desulfurization unit 170 has a sulfur-containing product gas inlet, a carbon-containing product gas outlet, and a sulfur product outlet. The sulfur-containing product gas inlet of the first desulfurization unit 170 is connected to the sulfur-containing product gas outlet of the conversion unit 160. The first desulfurization unit 170 is used to remove sulfides, such as H2S, from the sulfur-containing product gas.

[0088] The decarbonization unit 180 is used to remove carbon dioxide from the carbon-containing product gas to obtain the target product gas. The decarbonization unit 180 has a carbon-containing product gas inlet, a target product gas outlet, and a carbon dioxide outlet. The carbon-containing product gas inlet of the decarbonization unit 180 is connected to the carbon-containing product gas outlet of the first desulfurization unit 170, and the carbon dioxide outlet of the decarbonization unit 180 is connected to the auxiliary gas inlet of the gasification unit 110; the target product gas is output as the effective gas.

[0089] The second desulfurization unit 190 is used to desulfurize the flue gas generated by the combustion reaction in the boiler unit 120. The second desulfurization unit 190 is provided with a flue gas inlet and a flue gas outlet, and the flue gas inlet of the second desulfurization unit 190 is connected to the flue gas outlet of the boiler unit 120.

[0090] The above system can be applied to ammonia synthesis processes. In this scenario, the main products obtained by the gasification unit 110 include carbon monoxide, hydrogen, carbon dioxide, and nitrogen (derived from air). The carbon monoxide is further converted to hydrogen by the conversion unit 160. The outlet gas of the conversion unit 160 mainly includes carbon dioxide, hydrogen, and nitrogen. After decarbonization to remove carbon dioxide, the resulting product gas mainly includes hydrogen and nitrogen. The hydrogen and nitrogen can then be used in the ammonia synthesis process.

[0091] It should be noted that in this embodiment, the effective gas (mainly carbon monoxide and hydrogen) required by the user is mainly obtained through the gasification unit 110. The effective gas can be used in various synthesis processes and is not limited to the above-mentioned ammonia synthesis process.

[0092] Figure 3 A schematic diagram of a reaction control system according to yet another embodiment of the present disclosure is shown.

[0093] like Figure 3 As shown, Figure 3 The reaction control system shown is Figure 2 The reaction control systems shown are largely the same, differing only in that they also include a conveying unit for transporting carbonaceous fly ash to boiler unit 120. The conveying unit can be located between gasification unit 110 and boiler unit 120, or between dust removal unit 150 and boiler unit 120, or both between gasification unit 110 and boiler unit 120 and between dust removal unit 150 and boiler unit 120. The conveying unit can achieve pneumatic conveying of hot ash at temperatures between 100℃ and 250℃.

[0094] The conveying unit is equipped with a fly ash inlet and a fly ash outlet. For example, if the conveying unit is located between the gasification unit 110 and the boiler unit 120, the fly ash inlet of the conveying unit is connected to the carbonaceous fly ash outlet of the gasification unit 110. If the conveying unit is located between the dust removal unit 150 and the boiler unit 120, the fly ash inlet of the conveying unit is connected to the carbonaceous fly ash outlet of the dust removal unit 150.

[0095] According to embodiments of this disclosure, the conveying unit may further include a main powder delivery air duct, a first powder delivery air duct group, a second powder delivery air duct group, a powder delivery air mixer, and a fluidizing air duct.

[0096] The main pulverized air supply pipe includes a fly ash inlet, a pulverized air supply inlet, and a pulverized air supply outlet. The pulverized air supply outlet is connected to the feed port of the boiler, and the fly ash inlet is connected to the carbon-containing gasified fly ash outlet of the gasification unit and / or the carbon-containing fly ash outlet of the dust removal unit 150. The pulverized air supply can be coal gas, vented gas, nitrogen, carbon dioxide, air, flue gas, or a mixture of the above gases.

[0097] The first powder delivery air duct assembly is used to deliver the first powder delivery air, including at least one first powder delivery air branch pipe, wherein the first powder delivery air contains combustible components, and the first powder delivery air branch pipe is equipped with a first flow regulating valve and a first flow meter.

[0098] The second powder delivery air duct assembly is used to deliver the second powder delivery air, including at least one second powder delivery air branch pipe, wherein the second powder delivery air does not contain any combustible components, and the second powder delivery air branch pipe is equipped with a second flow regulating valve and a second flow meter.

[0099] The powder supply air mixer includes: a first inlet connected to at least one first powder supply air branch pipe; a second inlet connected to at least one second powder supply air branch pipe; and a mixing air outlet connected to the powder supply air inlet of the main powder supply air duct.

[0100] The fluidizing air duct includes a fluidizing air inlet and N fluidizing air outlets, wherein the N fluidizing air outlets are evenly distributed on the same side of the fluidizing air duct; the bottom of the powder delivery air main duct has N fluidizing holes, and the N fluidizing holes are connected to the N fluidizing air outlets one by one. The powder delivery air mixer also includes a branch port, which is connected to the fluidizing air inlet.

[0101] When fly ash enters the conveying unit from the fly ash inlet, the calorific value of the overall gas-solid mixture entering the pulverized air main can be selectively controlled by adjusting the flow regulating valve based on the current calorific value. Specifically, to ensure the ignition and combustion stability of the ash and slag after entering the boiler, the composition of the pulverized air needs to be adjusted in real time according to the calorific value of the fly ash.

[0102] For example, if the fly ash has a high calorific value, its current calorific value can meet the requirements for ignition stability and combustion stability, so the calorific value of the pulverized air supply is not a concern. Since the first pulverized air supply contains combustible components and has a high cost, to reduce this cost, the amount of the first pulverized air supplying the boiler unit 120 can be reduced by adjusting the first flow regulating valve, or the amount of the second pulverized air supplying the boiler unit 120 can be increased by simultaneously adjusting the second flow regulating valve.

[0103] For example, when the calorific value of fly ash is low, its current calorific value does not meet the requirements for ignition stability and combustion stability. To enhance the ignition and combustion characteristics of low-calorific-value ash after entering boiler unit 120, the calorific value of the pulverized air supply needs to be considered. Since the first pulverized air supply contains combustible components and has a high calorific value, the amount of the first pulverized air supplying the boiler unit 120 can be increased by adjusting the first flow regulating valve, or the amount of the second pulverized air supplying the boiler unit 120 can be decreased by simultaneously adjusting the second flow regulating valve.

[0104] It should be noted that in the powder air mixer, carbon dioxide, nitrogen, coal gas, and purge gas can be mixed with each other; air and flue gas can be mixed; carbon dioxide, air, flue gas, and nitrogen can be mixed with each other, but coal gas, purge gas, and flue gas or air cannot be mixed.

[0105] Based on the above system, another aspect of the present invention provides a reaction regulation method.

[0106] Figure 4 A flowchart illustrating a reaction regulation method according to an embodiment of the present disclosure is shown schematically.

[0107] like Figure 4 As shown, the reaction control method includes operations S410 to S450.

[0108] In operation S410, carbon-based raw materials, gasifying agents and auxiliary gases are introduced into gasification unit 110 so that after the carbon-based raw materials, gasifying agents and auxiliary gases undergo gasification reaction in gasification unit 110, dust-containing product gas at the first temperature is obtained, and carbon-containing gasification ash is generated at the same time.

[0109] According to embodiments of this disclosure, the gasifying agent includes oxygen and non-oxygen components. The oxygen component can be air, oxygen, etc.; the non-oxygen component can be steam, carbon dioxide, nitrogen, etc. The auxiliary gas includes water vapor and / or carbon dioxide. The main components of the dust-laden product gas include gaseous products such as carbon monoxide, carbon dioxide, and hydrogen; the main components of the carbon-containing gasification ash include unreacted carbon-containing fly ash, residue, and other solid products. The dust-laden product gas is output from the dust-laden product gas outlet of the gasification unit 110, and the carbon-containing gasification ash is output from the carbon-containing gasification ash outlet of the gasification unit 110.

[0110] In operation S420, carbon-containing gasification ash and oxidant are introduced into the furnace of boiler unit 120, and water at a predetermined temperature (e.g., 0 to 100°C) is introduced into the heat exchange tube bundle of boiler unit 120 so that the carbon-containing gasification ash and oxidant can undergo a combustion reaction in the furnace, and the heat generated by the combustion reaction is used to exchange heat with the water at the predetermined temperature in the heat exchange tube bundle to generate first steam.

[0111] According to an embodiment of this disclosure, the carbon-containing gasification ash and oxidant output from the carbon-containing gasification ash outlet of the gasification unit 110 undergo a combustion reaction in the furnace of the boiler unit 120, raising the temperature inside the boiler unit 120. Water at a predetermined temperature (e.g., 0-100°C) is introduced into the heat exchange tube bundle of the boiler unit 120. Under the condition of continuous temperature increase, the water in the heat exchange tube bundle is heated and evaporated to generate first steam.

[0112] In operation S430, the first steam generated by the boiler unit 120 is fed into the power generation unit 130 so that the heat energy of the first steam is converted into electrical energy through the power generation unit 130.

[0113] According to the embodiments of this disclosure, in the power generation unit 130, the thermal energy of the first steam is converted into electrical energy in any of the prior art methods, which will not be elaborated here.

[0114] In operation S440, the actual effective gas volume in the dust-laden product gas of gasification unit 110, the actual power generation of power generation unit, the effective gas volume demand information of users, and the power generation demand information of users are obtained in the current time period.

[0115] According to embodiments of this disclosure, the user's effective gas volume demand information and the user's power generation demand information can be obtained based on historical experience data and survey data. The user's effective gas volume demand information can include the effective gas volume required by the user within a certain period; the user's power generation demand information can include the power generation required by the user within a certain period. Since the effective gas is contained in the dust-containing product gas, the effective gas volume can be indirectly adjusted by adjusting the gas volume of the dust-containing product gas. Furthermore, it is also necessary to make targeted adjustments to the effective gas portion of the dust-containing product gas. The actual effective gas volume can be measured according to existing technologies, which will not be elaborated here.

[0116] In operation S450, the gasification reaction in gasification unit 110 is regulated based on predetermined adjustment parameters according to the actual effective gas quantity, actual power generation, effective gas quantity demand information, and power generation demand information.

[0117] According to embodiments of this disclosure, the required effective gas quantity is compared with the current actual effective gas quantity. If the user's required effective gas quantity is greater than the current actual effective gas quantity, the effective gas quantity needs to be increased by changing a predetermined adjustment parameter. Similarly, if the user's required power generation is greater than the current actual power generation, the power generation needs to be increased by changing the predetermined adjustment parameter. The reverse is also true. If, at the same time, the user's required effective gas quantity is greater than the actual effective gas quantity, but the user's required power generation is less than the actual power generation, the effective gas quantity can be increased and the power generation decreased by changing the predetermined adjustment parameter, thereby achieving effective energy saving while meeting both the user's effective gas quantity and power generation requirements.

[0118] According to embodiments of this disclosure, during the gasification process of carbon-based raw materials, by adjusting the content and proportions of the carbon-based raw materials, gasifying agent, and auxiliary gas, the direction of the gasification products towards gaseous or electrical products can be indirectly controlled, thereby meeting users' electricity or gas consumption needs while achieving energy conservation. Furthermore, by adjusting predetermined parameters (such as adjusting the amount of auxiliary gas entering or the proportions of its components), the gasification products can be further controlled to be produced towards effective gases (such as carbon monoxide and hydrogen) or towards steam / electricity. This method takes into account both the raw material and fuel properties of coal, realizing the conversion of matter and energy in the system. While optimizing the matching of gas and electricity production, it maximizes the conversion process between raw materials and products, achieving maximum economic and social benefits.

[0119] It should be noted that in this embodiment, the user's desired effective gas (mainly carbon monoxide and hydrogen) is mainly obtained through a gasification unit. This effective gas can then be used in various synthesis processes, such as ammonia synthesis. Specifically, by adding auxiliary gases (water vapor and / or carbon dioxide) to the gasification unit, the concentration of reactants in the H2O-C and CO2-C reaction processes can be increased, promoting the reaction and thus causing the gasification unit's output to shift towards carbon monoxide and hydrogen.

[0120] According to embodiments of this disclosure, the predetermined adjustment parameters include at least one of the following: the amount of carbon-based raw material fed, the equivalence ratio of the gasification unit, the component ratio of oxygen and non-oxygen components in the gasifying agent, the ratio of water vapor to carbon-based raw material, the ratio of carbon dioxide to carbon-based raw material, the total amount of gasifying agent fed, and the particle size of the carbon-based raw material.

[0121] According to embodiments of this disclosure, the change of the predetermined adjustment parameter can be to one of the parameters or any combination of parameters. The equivalence ratio of the gasification unit 110 is used to characterize the ratio of the amount of oxygen theoretically required for complete combustion of the carbon-based feedstock entering the gasification unit 110 to the amount of oxygen in the gasifying agent fed into the furnace.

[0122] According to embodiments of this disclosure, regulating the gasification reaction in the gasification unit 110 based on predetermined adjustment parameters, according to the actual effective gas quantity, actual power generation, effective gas quantity demand information, and power generation demand information, includes operations S11 and S12:

[0123] In operation S11, when the control direction is determined to be to increase the effective gas content in the dust-containing product gas or to decrease the power generation based on the actual effective gas content, actual power generation, effective gas content demand information, and power generation demand information, the adjustment is carried out by changing the equivalence ratio of the gasification unit 110. Specifically, the operation is to maintain the carbon-based raw material feed amount unchanged, maintain the component ratio of the gasifying agent unchanged, maintain the ratio of water vapor to carbon-based raw material unchanged, maintain the ratio of carbon dioxide to carbon-based raw material unchanged, and increase the total feed amount of the gasifying agent to reduce the equivalence ratio of the gasification unit 110.

[0124] In operation S12, if the control direction is determined to be to reduce the effective gas content in the dust-containing product gas or increase the power generation based on the actual effective gas content, actual power generation, effective gas content demand information, and power generation demand information, the adjustment is carried out by changing the equivalence ratio of the gasification unit 110. Specifically, the operation is to maintain the carbon-based raw material feed amount unchanged, maintain the component ratio of the gasifying agent unchanged, maintain the ratio of water vapor to carbon-based raw material unchanged, maintain the ratio of carbon dioxide to carbon-based raw material unchanged, and reduce the total feed amount of the gasifying agent to increase the equivalence ratio of the gasification unit 110.

[0125] According to embodiments of this disclosure, under the condition that the amount of carbon-based raw material fed remains unchanged, only increasing the total amount of gasifying agent feed reduces the equivalence ratio of gasification unit 110, resulting in high gasification conversion efficiency of the carbon-based raw material. Therefore, it increases the effective gas yield in the dust-containing product gas and reduces the yield of steam / electric products. Conversely, under the condition that the amount of carbon-based raw material fed remains unchanged, only decreasing the total amount of gasifying agent feed increases the equivalence ratio of gasification unit 110, resulting in low gasification conversion efficiency of the carbon-based raw material. Therefore, it reduces the effective gas yield in the dust-containing product gas and increases the yield of steam / electric products. The amount of carbon-based raw material fed can be 60% to 140% of the designed feed amount. Preferably, it can be 90% to 140%, for example, 60%, 70%, 90%, 100%, 120%, 140%, etc.

[0126] According to embodiments of this disclosure, regulating the gasification reaction in the gasification unit 110 based on predetermined adjustment parameters, according to the actual effective gas quantity, actual power generation, effective gas quantity demand information, and power generation demand information, further includes operations S13 and S14:

[0127] In operation S13, the gasification reaction temperature of the gasification unit 110 is monitored, and a safety warning command is generated if the gasification reaction temperature is greater than or equal to a first temperature threshold. The first temperature threshold is calculated based on the softening temperature of the carbon-containing gasification ash; for example, the first temperature threshold = softening temperature of the carbon-containing gasification ash - 150°C. To ensure operational safety, the maximum temperature must be kept below the first temperature threshold, for example, at least 150°C lower than the softening temperature of the carbon-based raw material ash.

[0128] In operation S14, the rate of change of calorific value of carbon-containing gasification ash is calculated as the gasification reaction temperature changes, and energy transfer analysis results are generated based on the rate of change of calorific value. The energy transfer analysis results are used to characterize whether more energy in the carbon-based raw material is transferred to the product gas or more energy is transferred to the steam / electricity product.

[0129] According to an embodiment of this disclosure, exemplarily, increasing the total amount of gasifying agent to reduce the equivalence ratio of gasification unit 110 is taken as an example. Monitoring the reaction temperature change of gasification unit 110, the highest temperature inside the reactor increases as the equivalence ratio decreases, and the highest temperature is more than 150°C lower than the softening temperature of the carbon-based raw material ash. The calorific value of the product gas and the carbon-containing gasification ash are measured separately. If the temperature increases by 50°C to 150°C, the calorific value of the carbon-containing gasification ash decreases by 500 kcal / kg to 2000 kcal / kg, and the effective gas conversion efficiency can increase by 5% to 20%. This proves that more energy in the carbon-based raw material is transferred to the effective gas. Therefore, without changing other conditions, simply increasing the total amount of gasifying agent can increase the effective gas yield and reduce the yield of steam / electric products.

[0130] According to embodiments of this disclosure, regulating the gasification reaction in the gasification unit 110 based on predetermined adjustment parameters, according to the actual effective gas quantity, actual power generation, effective gas quantity demand information, and power generation demand information, includes operations S21 and S22:

[0131] In operation S21, when the control direction is determined to be increasing the effective gas content in the dust-containing product gas based on the actual effective gas quantity, actual power generation, effective gas quantity demand information, and power generation demand information, the adjustment is made by changing the gasification load of the gasification unit 110. Specifically, the operation is performed as follows: maintaining the equivalence ratio of the gasification unit 110 unchanged, maintaining the component ratio of the gasifying agent unchanged, maintaining the ratio of water vapor to carbon-based raw materials unchanged, maintaining the ratio of carbon dioxide to carbon-based raw materials unchanged, increasing the feed amount of carbon-based raw materials, and increasing the total feed amount of the gasifying agent, thereby increasing the gasification load of the gasification unit 110. Increasing the gasification load of the gasification unit 110 includes the following two cases:

[0132] While increasing the amount of effective gas, the power generation is reduced. Specifically, the amount of carbon-based raw material and gasifying agent fed are increased simultaneously, which increases the gasification load and the effective gas conversion efficiency (the conversion efficiency of substances in the carbon-based raw material into effective gases CO and H2) is high. Therefore, the effective gas output is increased and the output of steam / electricity is reduced. The amount of carbon-based raw material fed can be 70% to 100% of the designed feed amount, preferably 70% to 90%, such as 70%, 80%, 90%, etc.

[0133] While increasing the effective gas quantity or keeping it constant, the power generation is increased. Specifically, the input of carbon-based feedstock and gasifying agent is increased simultaneously, increasing the gasification load, resulting in a lower effective gas conversion efficiency and an increase in the total amount of gasification residue. However, as the gasification load continues to increase, the total effective gas quantity increases. Therefore, whether the total effective gas quantity increases or remains constant, the output of steam / electricity is simultaneously increased. The input of carbon-based feedstock can be 80% to 140% of the design input. Preferably, it can be 90% to 140%, such as 90%, 100%, 120%, 140%, etc.

[0134] In operation S22, based on the actual effective gas quantity, actual power generation, effective gas quantity demand information, and power generation demand information, if the control direction is determined to be a decrease or no change in the effective gas quantity in the dust-containing product gas, while simultaneously reducing power generation, the gasification load of the gasification unit 110 is adjusted. Specifically, the following operations are performed: maintaining the equivalence ratio of the gasification unit 110 unchanged, maintaining the component ratio of the gasifying agent unchanged, maintaining the ratio of water vapor to carbon-based raw materials unchanged, maintaining the ratio of carbon dioxide to carbon-based raw materials unchanged, reducing the amount of carbon-based raw materials fed in, and reducing the total amount of gasifying agent fed in, thereby reducing the gasification load of the gasification unit 110.

[0135] Simultaneously reducing the input of carbon-based feedstock and gasifying agent decreases the gasification load, resulting in a lower or unchanged effective gas conversion efficiency, while also reducing the total amount of gasification residue. Therefore, the total effective gas output decreases, and the output of steam / electricity products also decreases. The input of carbon-based feedstock can be 50% to 100% of the designed input. Preferably, it can be 50% to 90%, for example, 50%, 60%, 70%, 80%, 90%, 100%, etc.

[0136] According to embodiments of this disclosure, regulating the gasification reaction in the gasification unit 110 based on predetermined adjustment parameters, according to the actual effective gas quantity, actual power generation, effective gas quantity demand information, and power generation demand information, includes operations S23 and S25:

[0137] During operation S23, the gasification reaction temperature and gasification load of the gasification unit 110 are monitored.

[0138] In operation S24, when the gasification reaction temperature is greater than or equal to a second temperature threshold (e.g., 900°C) and the gasification load of gasification unit 110 is greater than or equal to a predetermined load threshold (e.g., 90% of the design load), a first energy transfer analysis result is generated, wherein the first energy transfer analysis result is used to characterize that more energy in the carbon-based feedstock is transferred to the effective gas.

[0139] In operation S25, when the gasification reaction temperature is less than a second temperature threshold (e.g., 900°C) and the gasification load of gasification unit 110 is less than a predetermined load threshold (e.g., 90% of the design load), a second energy transfer analysis result is generated, wherein the second energy transfer analysis result is used to characterize that more energy in the carbon-based feedstock is transferred to the steam / electric products.

[0140] For example, if the control direction is determined to be reducing the effective gas quantity or increasing power generation, the gasification load of gasification unit 110 can be reduced compared to the original load by decreasing the input of carbon-based raw materials and the total input of gasifying agent. At this time, by monitoring the gasification reaction temperature and gasification load, if the maximum gasification temperature is below 900°C and the gasification load is below 90% of the design load, it indicates that more energy in the carbon-based raw materials is transferred to the steam / electricity products.

[0141] Conversely, if the highest gasification temperature is greater than or equal to 900℃ and the gasification load is greater than or equal to 90% of the design load, it proves that more energy in the carbon-based raw material is transferred to the effective gas. At this time, although the regulation is directed to reduce the amount of effective gas or increase the power generation, more energy in the carbon-based raw material is still transferred to the effective gas.

[0142] For example, if the original gasification load is 120% of the design load, by reducing the amount of carbon-based feedstock and the total amount of gasifying agent, the gasification load of gasification unit 110 is reduced to 110%. This adjustment aims to reduce the effective gas volume or increase power generation. However, the maximum gasification temperature is still greater than or equal to 900℃, and the gasification load is still greater than or equal to 90% of the design load, meaning more energy from the carbon-based feedstock is still transferred to the effective gas. If the gasification load of gasification unit 110 is reduced to 80% through adjustment, the maximum gasification temperature is less than 900℃, and more energy from the carbon-based feedstock is transferred to steam / electricity products.

[0143] According to embodiments of this disclosure, the gasification reaction in the gasification unit 110 is regulated based on predetermined adjustment parameters according to the actual effective gas quantity, actual power generation, effective gas quantity demand information, and power generation demand information, including operations S31 to S32:

[0144] In operation S31, when the control direction is determined to be to increase the effective gas content in the dust-containing product gas or to decrease the power generation based on the actual effective gas content, actual power generation, effective gas content demand information, and power generation demand information, the operation is performed by changing the component ratio of the oxygen component: maintaining the equivalent ratio of the gasification unit 110 unchanged, maintaining the feed amount of carbon-based raw materials unchanged, maintaining the ratio of water vapor to carbon-based raw materials unchanged, maintaining the ratio of carbon dioxide to carbon-based raw materials unchanged, increasing the component ratio of the oxygen component in the gasifying agent, and decreasing the total feed amount of the gasifying agent.

[0145] In operation S32, when the control direction is determined to be to reduce the effective gas content in the dust-containing product gas or increase the power generation based on the actual effective gas content, actual power generation, effective gas content demand information, and power generation demand information, the operation is performed by changing the component ratio of the oxygen component: maintaining the equivalent ratio of the gasification unit 110 unchanged, maintaining the feed amount of carbon-based raw materials unchanged, maintaining the ratio of water vapor to carbon-based raw materials unchanged, maintaining the ratio of carbon dioxide to carbon-based raw materials unchanged, reducing the component ratio of the oxygen component in the gasifying agent, and increasing the total feed amount of the gasifying agent.

[0146] For example, by increasing the proportion of oxygen in the gasifying agent, the oxygen concentration in the gasifying agent increases from 21% to 35%–55%, the carbon conversion rate of gasification unit 110 increases, the calorific value of gasification residue decreases by 500 kcal / kg–1000 kcal / kg, the effective gas conversion efficiency increases by 5%–10%, and more energy in the carbon-based raw material is transferred to the effective gas, thereby increasing the effective gas production and reducing the production of steam / electric products.

[0147] According to embodiments of this disclosure, the gasification reaction in the gasification unit 110 is regulated based on predetermined adjustment parameters according to the actual effective gas quantity, actual power generation, effective gas quantity demand information, and power generation demand information, including operations S41 to S45:

[0148] In operation S41, if the control direction is determined to be either reducing the effective gas quantity or increasing the power generation based on the actual effective gas quantity, actual power generation, effective gas quantity demand information, and power generation demand information, the adjustment is made by changing the particle size of the carbon-based raw material, and the following operations are performed:

[0149] In operation S42, the equivalence ratio of gasification unit 110 is kept constant, the amount of carbon-based feedstock is kept constant, the component ratio of gasifying agent is kept constant, the ratio of water vapor to carbon-based feedstock is kept constant, the ratio of carbon dioxide to carbon-based feedstock is kept constant, and the total amount of gasifying agent is kept constant.

[0150] In operation S43, the current value of the particle size of the carbon-based raw material is measured;

[0151] In operation S44, if the current value of the particle size of the carbon-based raw material is less than the first reference value, the particle size of the carbon-based raw material introduced into the gasification unit 110 is reduced, wherein the first reference value is calculated based on the median particle size of fly ash at the outlet of the cyclone separator of the gasification unit 110.

[0152] According to embodiments of this disclosure, the first reference value can be 20 times the median particle size of the fly ash at the outlet of the cyclone separator in the gasification unit 110. By reducing the particle size of the carbon-based feedstock, the residence time of the carbon-based feedstock in the reactor is shortened due to the influence of fluidization velocity and cyclone separator separation efficiency, resulting in a decrease in carbon conversion rate and more energy being transferred to the carbon-containing gasified fly ash, thereby reducing the effective gas yield and increasing the yield of steam / electricity products.

[0153] In operation S45, if the current value of the particle size of the carbon-based raw material is greater than the second reference value, the particle size of the carbon-based raw material introduced into the gasification unit 110 is increased, wherein the second reference value is calculated based on the median particle size of fly ash at the outlet of the cyclone separator of the gasification unit 110.

[0154] According to embodiments of this disclosure, the second reference value is greater than the first reference value. The second reference value can be 50 times the median particle size of the fly ash at the outlet of the cyclone separator in gasification unit 110. By increasing the particle size of the carbon-based raw material, the specific surface area of ​​the coal is relatively small, resulting in insufficient gas-solid contact and slow heat and mass transfer between the particles, which affects the heterogeneous gasification reaction, reduces the carbon conversion rate, and transfers more energy to the carbon-containing gasification ash, thereby reducing the effective gas yield and increasing the yield of steam / electricity products.

[0155] According to embodiments of this disclosure, the gasification reaction in the gasification unit is regulated based on predetermined adjustment parameters according to the actual effective gas quantity, actual power generation, effective gas quantity demand information, and power generation demand information, including operations S51 to S52:

[0156] In operation S51, based on the actual effective gas quantity, actual power generation, effective gas quantity demand information, and power generation demand information, if the control direction is determined to be to increase the effective gas quantity in the dust-containing product gas or to decrease the power generation, the adjustment is made by changing the equivalence ratio of the gasification unit 110 and simultaneously changing the ratio of water vapor to carbon-based raw materials. Specifically, the operation is as follows: the feed amount of carbon-based raw materials remains unchanged, the proportion of oxygen components in the gasifying agent remains unchanged, the ratio of carbon dioxide to carbon-based raw materials remains unchanged, the equivalence ratio of the gasification unit is decreased, the ratio of water vapor to carbon-based raw materials is increased, and the gasification temperature remains unchanged.

[0157] For example, consider reducing the equivalence ratio of the gasification unit while increasing the ratio of water vapor to carbon-based feedstock. On the one hand, reducing the equivalence ratio helps to enhance the C-O2 reaction, increasing the heat released by the reaction to support the endothermic reactions related to gasification; on the other hand, increasing the water vapor, by increasing the reactant concentration, can effectively promote the C-H2O reaction and increase the yield of hydrogen in the product.

[0158] In operation S52, based on the actual effective gas quantity, actual power generation, effective gas quantity demand information, and power generation demand information, if the control direction is determined to be reducing the effective gas quantity in the dust-containing product gas or increasing power generation, the adjustment is made by changing the equivalence ratio of the gasification unit 110 and simultaneously changing the ratio of water vapor to carbon-based raw materials. Specifically, the operation is as follows: the amount of carbon-based raw materials fed in remains unchanged, the proportion of oxygen components in the gasifying agent remains unchanged, the ratio of carbon dioxide to carbon-based raw materials remains unchanged, the equivalence ratio of the gasification unit is increased, the ratio of water vapor to carbon-based raw materials is decreased, and the gasification temperature remains unchanged.

[0159] According to embodiments of this disclosure, the gasification reaction in the gasification unit is regulated based on predetermined adjustment parameters according to the actual effective gas quantity, actual power generation, effective gas quantity demand information, and power generation demand information, including operations S61 to S62:

[0160] In operation S61, based on the actual effective gas quantity, actual power generation, effective gas quantity demand information, and power generation demand information, if the control direction is determined to be to increase the effective gas quantity in the dust-containing product gas or to decrease the power generation, the adjustment is made by changing the equivalence ratio of the gasification unit 110 and simultaneously changing the ratio of carbon dioxide to carbon-based raw materials. Specifically, the operation is as follows: the amount of carbon-based raw materials fed in remains constant, the proportion of oxygen components in the gasifying agent remains constant, the ratio of water vapor to carbon-based raw materials remains constant, the equivalence ratio of the gasification unit is decreased, the ratio of carbon dioxide to carbon-based raw materials is increased, and the gasification temperature remains constant.

[0161] For example, consider reducing the equivalence ratio of the gasification unit while increasing the ratio of carbon dioxide to carbon-based feedstock. On the one hand, reducing the equivalence ratio helps to enhance the C-O2 reaction, increasing the heat released by the reaction to support the endothermic reactions related to gasification; on the other hand, increasing carbon dioxide, by increasing the reactant concentration, can effectively promote the C-CO2 reaction and increase the yield of carbon monoxide in the product.

[0162] In operation S62, based on the actual effective gas quantity, actual power generation, effective gas quantity demand information, and power generation demand information, if the control direction is determined to be reducing the effective gas quantity in the dust-containing product gas or increasing power generation, the adjustment is made by changing the equivalence ratio of the gasification unit 110 and simultaneously changing the ratio of carbon dioxide to carbon-based raw materials. Specifically, the operation is as follows: the amount of carbon-based raw materials fed in remains constant, the proportion of oxygen components in the gasifying agent remains constant, the ratio of water vapor to carbon-based raw materials remains constant, the equivalence ratio of the gasification unit is increased, the ratio of carbon dioxide to carbon-based raw materials is decreased, and the gasification temperature remains constant.

[0163] Furthermore, during the above-mentioned control process, the gasification reaction temperature of the gasification unit is monitored, and a safety warning command is generated when the gasification reaction temperature is greater than or equal to a first temperature threshold. The first temperature threshold is calculated based on the softening temperature of the carbon-containing gasification ash (the gasification temperature is controlled to be more than 150°C lower than the softening temperature of the carbon-based raw material ash, and preferably, the gasification temperature is higher than 1000°C).

[0164] According to embodiments of this disclosure, in any of the above-described control strategies, the change in the reaction fluidization velocity of the gasification unit 110 can be monitored in real time, so that the fluidization velocity at the bottom of the furnace is not less than 1 m / s, and the fluidization velocity is not too low, so as not to affect the stability and safety of operation.

[0165] Figure 5 A flowchart illustrating another embodiment of the reaction regulation method of this disclosure is shown schematically.

[0166] like Figure 5 As shown, the reaction control method includes operations S510 to S580.

[0167] In operation S510, dust-laden product gas at a first temperature and water at a predetermined temperature are introduced into the waste heat recovery unit 140 so that the dust-laden product gas at the first temperature and the water at the predetermined temperature exchange heat in the waste heat recovery unit 140 to obtain dust-laden product gas at a second temperature and second steam.

[0168] According to embodiments of this disclosure, dust-laden product gas exiting from the dust-laden product gas outlet of the gasification unit 110 enters the waste heat recovery unit 140 through the dust-laden product gas inlet. Simultaneously, water at a predetermined temperature (e.g., 0–100°C) is introduced into the heat exchange tube bundle of the waste heat recovery unit 140. The dust-laden product gas undergoes indirect heat exchange with water in the waste heat recovery unit 140, heating the water into steam to obtain a second steam; or the dust-laden product gas first exchanges heat with a gasifying agent, then with water, heating the water into steam to obtain a second steam. The dust-laden product gas at the second temperature after heat exchange with water exits from the dust-laden product gas outlet of the waste heat recovery unit 140. The second steam is output from the second steam outlet of the waste heat recovery unit 140.

[0169] In operation S520, the second steam is introduced into the power generation unit 130 so that the thermal energy of the second steam and the first steam is converted into electrical energy through the power generation unit 130.

[0170] According to embodiments of this disclosure, the second steam output from the second steam outlet of the waste heat recovery unit 140 can be directly transmitted to the power generation unit 130 to drive the steam turbine to generate electricity; it can also enter the gasification unit 110 to participate in the gasification reaction, which helps to improve the gasification efficiency; or it can enter the conversion unit 160.

[0171] In operation S530, the dust-laden product gas at the second temperature is introduced into the dust removal unit 150 for gas-solid separation to obtain dust-free product gas and carbon-containing fly ash.

[0172] According to embodiments of this disclosure, the dust-laden product gas output from the dust-laden product gas outlet of the waste heat recovery unit 140 enters the dust removal unit 150 through the dust-laden product gas inlet. In the dust removal unit 150, the product gas and carbon-containing fly ash are separated. The dust-free product gas is discharged from the dust-free product gas outlet of the dust removal unit 150, and the carbon-containing fly ash is discharged from the carbon-containing fly ash outlet of the dust removal unit 150. The ash leaving the dust removal unit 150 is hot ash at 100℃~250℃. Specifically, it can be 100℃, 150℃, 200℃, 220℃, etc.

[0173] In operation S540, carbon-containing fly ash is introduced into the furnace of boiler unit 120 so that the carbon-containing fly ash and carbon-containing gasification ash are burned together as fuel in the furnace.

[0174] According to an embodiment of this disclosure, carbonaceous fly ash that has undergone dust removal is discharged from the carbonaceous fly ash outlet of the dust removal unit 150 and enters the boiler unit 120 through the carbonaceous fly ash inlet of the boiler unit 120 for combustion as fuel.

[0175] In operation S550, dust-free product gas is introduced into conversion unit 160 for gas conversion to obtain sulfur-containing product gas. The conversion reaction includes: carbon monoxide in the dust-free product gas reacts with water vapor introduced into the conversion unit to generate carbon dioxide and hydrogen.

[0176] According to an embodiment of this disclosure, the dust-free product gas, after dust removal, is discharged from the dust-free product gas outlet of the dust removal unit 150 and enters the conversion unit 160 through the dust-free product gas inlet. After a conversion reaction, sulfur-containing product gas is generated. The sulfur-containing product gas is discharged from the sulfur-containing product gas outlet of the conversion unit 160.

[0177] In operation S560, sulfur-containing product gas is introduced into the first desulfurization unit 170 for sulfide recovery, resulting in carbon-containing product gas and sulfur product.

[0178] According to embodiments of this disclosure, sulfur-containing product gas discharged from the sulfur-containing product gas outlet of the conversion unit 160 enters the first desulfurization unit 170 through the sulfur-containing product gas inlet and undergoes sulfide recovery to remove sulfides, such as H2S, from the sulfur-containing product gas. The sulfur obtained from desulfurization is output as a product; the carbon-containing product gas is output.

[0179] In operation S570, carbon-containing product gas is passed into decarbonization unit 180 to remove carbon dioxide and obtain target product gas. The removed carbon dioxide can be used for gasification in gasification unit 110.

[0180] According to an embodiment of this disclosure, the carbon-containing product gas output from the first desulfurization unit 170 enters the decarbonization unit 180 through the carbon-containing product gas inlet of the decarbonization unit 180, and after decarbonization, carbon dioxide is discharged; the remaining gas is output as the target product gas, wherein the target product gas contains at least carbon monoxide and hydrogen.

[0181] In operation S580, the flue gas generated by the combustion reaction in boiler unit 120 is introduced into the second desulfurization unit 190 for desulfurization.

[0182] According to an embodiment of this disclosure, the flue gas output from boiler unit 120 can enter the second desulfurization unit 190, undergo desulfurization treatment, and then be directly discharged.

[0183] The above method can be applied to the process of ammonia synthesis. In this scenario, the main products obtained from the gasification unit include carbon monoxide, hydrogen, carbon dioxide, and nitrogen (derived from air). The carbon monoxide is further converted to hydrogen by a shift conversion unit. The outlet gas from the shift conversion unit mainly consists of carbon dioxide, hydrogen, and nitrogen. After decarbonization to remove carbon dioxide, the resulting product gas mainly contains hydrogen and nitrogen. The hydrogen and nitrogen can then be used in the ammonia synthesis process.

[0184] It should be noted that in this embodiment, the effective gas (mainly carbon monoxide and hydrogen) required by the user is mainly obtained through the gasification unit. The effective gas can be used in various synthesis processes and is not limited to the above-mentioned ammonia synthesis process.

[0185] The specific embodiments described above further illustrate the purpose, technical solution, and beneficial effects of the present invention. It should be understood that the above descriptions are merely specific embodiments of the present invention and are not intended to limit the present invention. Any modifications, equivalent substitutions, improvements, etc., made within the spirit and principles of the present invention should be included within the protection scope of the present invention.

Claims

1. A reaction control method, comprising: Carbon-based raw materials, gasifying agents, and auxiliary gases are introduced into a gasification unit so that the carbon-based raw materials, the gasifying agents, and the auxiliary gases undergo a gasification reaction in the gasification unit to obtain dust-containing product gas at a first temperature, while generating carbon-containing gasification ash slag. The dust-containing product gas includes effective gases for the gas synthesis process. The carbon-containing gasification ash and oxidant are introduced into the furnace of the boiler unit, and water at a predetermined temperature is introduced into the heat exchange tube bundle of the boiler unit so that the carbon-containing gasification ash and oxidant can undergo a combustion reaction in the furnace, and the heat generated by the combustion reaction can be used to exchange heat with the water at a predetermined temperature in the heat exchange tube bundle to generate the first steam. The first steam generated by the boiler unit is fed into the power generation unit so that the heat energy of the first steam is converted into electrical energy by the power generation unit. Obtain the actual effective gas volume in the dust-laden product gas of the gasification unit, the actual power generation of the power generation unit, the effective gas volume demand information of the user, and the power generation demand information of the user in the current time period; Based on the actual effective gas quantity, the actual power generation, the effective gas quantity demand information, and the power generation demand information, the gasification reaction in the gasification unit is regulated according to predetermined adjustment parameters; The auxiliary gas includes water vapor and / or carbon dioxide; The dust-containing product gas includes at least carbon monoxide, hydrogen, and carbon dioxide, wherein the effective gas in the dust-containing product gas includes at least carbon monoxide and hydrogen; The vaporizing agent includes oxygen components and non-oxygen components; The predetermined adjustment parameters include at least one of the following: the amount of carbon-based raw material fed, the equivalence ratio of the gasification unit, the component ratio of the oxygen component and the non-oxygen component in the gasifying agent, the ratio of water vapor to the carbon-based raw material, the ratio of carbon dioxide to the carbon-based raw material, the total amount of the gasifying agent fed, and the particle size of the carbon-based raw material.

2. The method according to claim 1, wherein, Based on the actual effective gas quantity, the actual power generation, the effective gas quantity demand information, and the power generation demand information, regulating the gasification reaction in the gasification unit according to predetermined adjustment parameters includes: If, based on the actual effective gas quantity, the actual power generation, the effective gas quantity demand information, and the power generation demand information, it is determined that the control direction is to increase the effective gas quantity in the dust-containing product gas or decrease the power generation, the following operations are performed: maintaining the feed amount of the carbon-based raw material unchanged, maintaining the component ratio of the gasifying agent unchanged, maintaining the ratio of water vapor to the carbon-based raw material unchanged, maintaining the ratio of carbon dioxide to the carbon-based raw material unchanged, and increasing the total feed amount of the gasifying agent to reduce the equivalence ratio of the gasification unit; If, based on the actual effective gas quantity, the actual power generation, the effective gas quantity demand information, and the power generation demand information, it is determined that the control direction is to reduce the effective gas quantity in the dust-containing product gas or increase the power generation, the following operations are performed: maintaining the feed amount of the carbon-based raw material unchanged, maintaining the component ratio of the gasifying agent unchanged, maintaining the ratio of water vapor to the carbon-based raw material unchanged, maintaining the ratio of carbon dioxide to the carbon-based raw material unchanged, and reducing the total feed amount of the gasifying agent to increase the equivalence ratio of the gasification unit.

3. The method according to claim 2, further comprising: The gasification reaction temperature of the gasification unit is monitored, and a safety warning command is generated when the gasification reaction temperature is greater than or equal to a first temperature threshold, wherein the first temperature threshold is calculated based on the softening temperature of the carbon-containing gasification ash. The rate of change of calorific value of the carbon-containing gasification ash is calculated as a function of gasification reaction temperature, and an energy transfer analysis result is generated based on the rate of change of calorific value. The energy transfer analysis result is used to characterize whether more energy in the carbon-based raw material is transferred to the product gas or to the steam / electricity product.

4. The method according to claim 1, wherein, Based on the actual effective gas quantity, the actual power generation, the effective gas quantity demand information, and the power generation demand information, regulating the gasification reaction in the gasification unit according to predetermined adjustment parameters includes: If, based on the actual effective gas quantity, the actual power generation, the effective gas quantity demand information, and the power generation demand information, it is determined that the control direction is to increase the effective gas quantity in the dust-containing product gas, the following operations are performed: maintaining the equivalence ratio of the gasification unit unchanged, maintaining the component ratio of the gasifying agent unchanged, maintaining the ratio of water vapor to carbon-based raw material unchanged, maintaining the ratio of carbon dioxide to carbon-based raw material unchanged, increasing the feed amount of carbon-based raw material, and increasing the total feed amount of the gasifying agent, thereby increasing the gasification load of the gasification unit; If, based on the actual effective gas quantity, the actual power generation, the effective gas quantity demand information, and the power generation demand information, the control direction is determined to be reducing the effective gas quantity in the dust-containing product gas, the following operations are performed: maintaining the equivalence ratio of the gasification unit unchanged, maintaining the component ratio of the gasifying agent unchanged, maintaining the ratio of water vapor to carbon-based raw materials unchanged, maintaining the ratio of carbon dioxide to carbon-based raw materials unchanged, reducing the feed amount of carbon-based raw materials, and reducing the total feed amount of the gasifying agent, thereby reducing the gasification load of the gasification unit.

5. The method according to claim 4, further comprising: Monitor the gasification reaction temperature and the gasification load of the gasification unit; When the gasification reaction temperature is greater than or equal to a second temperature threshold and the gasification load of the gasification unit is greater than or equal to a predetermined load threshold, a first energy transfer analysis result is generated, wherein the first energy transfer analysis result is used to characterize that more energy in the carbon-based raw material is transferred to the product gas; When the gasification reaction temperature is less than the second temperature threshold and the gasification load of the gasification unit is less than the predetermined load threshold, a second energy transfer analysis result is generated, wherein the second energy transfer analysis result is used to characterize that more energy in the carbon-based raw material is transferred to the steam / electric product.

6. The method according to claim 1, wherein, Based on the actual effective gas quantity, the actual power generation, the effective gas quantity demand information, and the power generation demand information, regulating the gasification reaction in the gasification unit according to predetermined adjustment parameters includes: If, based on the actual effective gas quantity, the actual power generation, the effective gas quantity demand information, and the power generation demand information, it is determined that the control direction is to increase the effective gas quantity in the dust-containing product gas or decrease the power generation, the following operations are performed: maintaining the equivalence ratio of the gasification unit unchanged, maintaining the feed amount of the carbon-based raw material unchanged, maintaining the ratio of water vapor to the carbon-based raw material unchanged, maintaining the ratio of carbon dioxide to the carbon-based raw material unchanged, increasing the component proportion of oxygen in the gasifying agent, and decreasing the total feed amount of the gasifying agent; If, based on the actual effective gas quantity, the actual power generation, the effective gas quantity demand information, and the power generation demand information, it is determined that the control direction is to reduce the effective gas quantity in the dust-containing product gas or increase the power generation, the following operations are performed: maintaining the equivalence ratio of the gasification unit unchanged, maintaining the feed amount of the carbon-based raw material unchanged, maintaining the ratio of water vapor to the carbon-based raw material unchanged, maintaining the ratio of carbon dioxide to the carbon-based raw material unchanged, reducing the component proportion of oxygen in the gasifying agent, and increasing the total feed amount of the gasifying agent.

7. The method according to claim 1, wherein, Based on the actual effective gas quantity, the actual power generation, the effective gas quantity demand information, and the power generation demand information, regulating the gasification reaction in the gasification unit according to predetermined adjustment parameters includes: Based on the actual effective gas quantity, the actual power generation, the effective gas quantity demand information, and the power generation demand information, if the control direction is determined to be reducing the effective gas quantity in the dust-containing product gas or increasing power generation, the following operations are performed: The equivalence ratio of the gasification unit is kept constant, the amount of carbon-based raw material fed is kept constant, the component ratio of the gasifying agent is kept constant, the ratio of water vapor to carbon-based raw material is kept constant, the ratio of carbon dioxide to carbon-based raw material is kept constant, and the total amount of gasifying agent fed is kept constant. The current value of the particle size of the carbon-based raw material is measured; If the current value of the particle size of the carbon-based raw material is less than a first reference value, the particle size of the carbon-based raw material introduced into the gasification unit is reduced, wherein the first reference value is calculated based on the median particle size of fly ash at the outlet of the cyclone separator of the gasification unit. If the current value of the particle size of the carbon-based raw material is greater than the second reference value, the particle size of the carbon-based raw material introduced into the gasification unit is increased, wherein the second reference value is calculated based on the median particle size of fly ash at the outlet of the cyclone separator of the gasification unit, and the second reference value is greater than the first reference value.

8. The method according to claim 1, wherein, Based on the actual effective gas quantity, the actual power generation, the effective gas quantity demand information, and the power generation demand information, regulating the gasification reaction in the gasification unit according to predetermined adjustment parameters includes: Based on the actual effective gas quantity, the actual power generation, the effective gas quantity demand information, and the power generation demand information, if the control direction is determined to be increasing the effective gas quantity in the dust-containing product gas or decreasing the power generation, the following operations are performed: maintaining the feed amount of the carbon-based raw material unchanged, maintaining the proportion of oxygen components in the gasifying agent unchanged, maintaining the ratio of carbon dioxide to the carbon-based raw material unchanged, decreasing the equivalence ratio of the gasification unit, increasing the ratio of water vapor to the carbon-based raw material, and maintaining the gasification temperature unchanged; Based on the actual effective gas quantity, the actual power generation, the effective gas quantity demand information, and the power generation demand information, if the control direction is determined to be reducing the effective gas quantity in the dust-containing product gas or increasing the power generation, the following operations are performed: maintaining the feed amount of the carbon-based raw material unchanged, maintaining the proportion of oxygen components in the gasifying agent unchanged, maintaining the ratio of carbon dioxide to the carbon-based raw material unchanged, increasing the equivalence ratio of the gasification unit, decreasing the ratio of water vapor to the carbon-based raw material, and maintaining the gasification temperature unchanged.

9. The method according to claim 1, wherein, Based on the actual effective gas quantity, the actual power generation, the effective gas quantity demand information, and the power generation demand information, regulating the gasification reaction in the gasification unit according to predetermined adjustment parameters includes: Based on the actual effective gas quantity, the actual power generation, the effective gas quantity demand information, and the power generation demand information, if the control direction is determined to be increasing the effective gas quantity in the dust-containing product gas or decreasing the power generation, the following operations are performed: maintaining the feed amount of the carbon-based raw material unchanged, maintaining the proportion of oxygen components in the gasifying agent unchanged, maintaining the ratio of water vapor to the carbon-based raw material unchanged, decreasing the equivalence ratio of the gasification unit, increasing the ratio of carbon dioxide to the carbon-based raw material, and maintaining the gasification temperature unchanged; Based on the actual effective gas quantity, the actual power generation, the effective gas quantity demand information, and the power generation demand information, if the control direction is determined to be reducing the effective gas quantity in the dust-containing product gas or increasing the power generation, the following operations are performed: maintaining the feed amount of the carbon-based raw material unchanged, maintaining the proportion of oxygen components in the gasifying agent unchanged, maintaining the ratio of water vapor to the carbon-based raw material unchanged, increasing the equivalence ratio of the gasification unit, decreasing the ratio of carbon dioxide to the carbon-based raw material, and maintaining the gasification temperature unchanged.

10. The method according to claim 1, further comprising: The dust-laden product gas at the first temperature and the water at the predetermined temperature are introduced into the waste heat recovery unit so that the dust-laden product gas at the first temperature and the water at the predetermined temperature exchange heat in the waste heat recovery unit to obtain the dust-laden product gas at the second temperature and the second steam. The second steam is introduced into the power generation unit so that the thermal energy of the second steam and the first steam can be converted into electrical energy through the power generation unit; The dust-laden product gas at the second temperature is passed into the dust removal unit for gas-solid separation to obtain dust-free product gas and carbon-containing fly ash. The carbon-containing fly ash is introduced into the furnace of the boiler unit so that the carbon-containing fly ash and the carbon-containing gasification ash are burned together as fuel in the furnace. The dust-free product gas is passed into a conversion unit for gas conversion to obtain sulfur-containing product gas. The conversion includes: carbon monoxide in the dust-free product gas reacts with water vapor passed into the conversion unit to generate carbon dioxide and hydrogen. The sulfur-containing product gas is passed into the first desulfurization unit for sulfide recovery, resulting in carbon-containing product gas and sulfur product. The carbon-containing product gas is passed into a decarbonization unit to remove carbon dioxide, thereby obtaining the target product gas. The removed carbon dioxide can be used for gasification in the gasification unit. The flue gas generated by the combustion reaction in the boiler unit is passed into the second desulfurization unit for desulfurization.

11. A reaction control system, comprising: A gasification unit is used to react carbon-based raw materials, gasification agents, and auxiliary gases in the gasification unit to obtain dust-containing product gas at a first temperature, while generating carbon-containing gasification ash slag. The dust-containing product gas includes effective gases for gas synthesis processes. A boiler unit is used for the combustion reaction of the carbon-containing gasified ash and oxidant in the furnace of the boiler unit, and the heat generated by the combustion reaction is exchanged with water at a predetermined temperature in the heat exchange tube bundle of the boiler unit to generate first steam. A power generation unit is used to convert the thermal energy of the first steam into electrical energy. The control unit is used to acquire, during the current time period, the actual effective gas quantity in the dust-containing product gas of the gasification unit, the actual power generation of the power generation unit, the effective gas quantity demand information of the user, and the power generation demand information of the user, and to control the gasification reaction in the gasification unit based on the actual effective gas quantity, the actual power generation, the effective gas quantity demand information, and the power generation demand information, according to predetermined control parameters. The auxiliary gas includes water vapor and / or carbon dioxide; The dust-containing product gas includes at least carbon monoxide, hydrogen, and carbon dioxide, wherein the effective gas in the dust-containing product gas includes at least carbon monoxide and hydrogen; The vaporizing agent includes oxygen components and non-oxygen components; The predetermined adjustment parameters include at least one of the following: the amount of carbon-based raw material fed, the equivalence ratio of the gasification unit, the component ratio of the oxygen component and the non-oxygen component in the gasifying agent, the ratio of water vapor to the carbon-based raw material, the ratio of carbon dioxide to the carbon-based raw material, the total amount of the gasifying agent fed, and the particle size of the carbon-based raw material.

12. The system according to claim 11, further comprising: The waste heat recovery unit is used to exchange heat between the dust-laden product gas at the first temperature and water at a predetermined temperature to obtain dust-laden product gas at the second temperature and second steam, wherein the second steam is fed into the power generation unit. The dust removal unit is used to perform gas-solid separation on the dust-containing product gas at the second temperature to obtain dust-free product gas and carbon-containing fly ash, wherein the carbon-containing fly ash is introduced into the furnace of the boiler unit. A conversion unit is used to convert the dust-free product gas into sulfur-containing product gas after a conversion reaction, wherein the conversion reaction includes: carbon monoxide in the dust-free product gas reacting with water vapor introduced into the conversion unit to generate carbon dioxide and hydrogen. The first desulfurization unit is used to recover sulfides from the sulfur-containing product gas to obtain carbon-containing product gas and sulfur products. A decarbonization unit is used to remove carbon dioxide from the carbon-containing product gas to obtain the target product gas. The second desulfurization unit is used to desulfurize the flue gas generated by the combustion reaction in the boiler unit.

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