WO2023044859A1 - High-temperature clean gasification apparatus and method for achieving high carbon conversion rate of carbon-containing materials - Google Patents

Abstract

A two-stage melting gasification furnace (100) and method for harmlessly disposing carbon-containing materials. The furnace comprises a horizontal reaction section (100A) and a vertical reaction section (100B) in fluid communication, and the latter is located above the former and connected to the former by means of a connection port (E). The horizontal reaction section sequentially comprises a low-carbon slag section (A), a high-carbon slag section (B), and a gas-phase reaction section (C) from bottom to top. The vertical reaction section comprises a cooling reduction section (D). The low-carbon slag section (A) comprises first gasifying agent inlets (121, 122, 123), a first slag combustion-supporting gas inlet (1), a second slag combustion-supporting gas inlet (11) and a liquid slag discharging port (10). Under normal operating conditions, pyrolytic carbon particles falling into the low-carbon slag section have cohesiveness or flowability due to the fact that carbon content is lower than a threshold. The high-carbon slag section (B) comprises a second gasifying agent inlet (2). Under normal operating conditions, pyrolytic carbon particles falling into the high-carbon slag section do not have cohesiveness or flowability due to the fact that the carbon content is higher than the threshold. The gas-phase reaction section (C) comprises a carbon-containing material inlet (3), a third gasifying agent inlet (9), and a carbon-containing fine powder inlet (8). Under normal operating conditions, the carbon-containing materials fed into the gas-phase reaction section are pyrolyzed, some of the pyrolyzed products undergo a redox reaction, and the generated gas phase enters the cooling reduction section (D) by means of the connection port (E). The cooling reduction section (D) comprises a cooling device configured to reduce the temperature inside the section, and a high-temperature raw synthesis gas outlet (6). Under normal operating conditions, CO2, H2O, and carbon in carbon-containing fly ash in the gas entering the cooling reduction section undergo a reduction reaction to generate CO and H2. FIG. 1

Description

A high-temperature clean gasification device and method for realizing high carbon conversion rate of carbon-containing materials technical field

This application relates to the technical field of harmless disposal of carbonaceous materials, in particular to a high-temperature clean gasification device and method for realizing high carbon conversion rate of carbonaceous materials.

Background technique

Carbon-containing materials widely exist in nature, including naturally formed coal, petroleum, and trees, as well as artificially synthesized plastics, rubber, domestic garbage, and organic hazardous waste. Wastes that have lost their use value after human use often need to be disposed of in an appropriate way to avoid harming the environment. In particular, hazardous wastes often have hazardous characteristics such as corrosiveness, toxicity, flammability, reactivity, and infectivity. Improper use and disposal will seriously endanger human health, and even cause irreversible damage to the ecological environment. At present, the operation and technical level of hazardous waste utilization and disposal facilities need to be improved, and there is a phenomenon of excessive discharge, especially the pollution of hazardous waste containing heavy metals.

The current disposal methods of hazardous waste include landfill, incineration, co-processing of cement furnace and kiln, and plasma melting. Among them, landfill needs to occupy a large amount of land and is likely to cause land pollution; incineration has incomplete disposal and secondary pollution of flue gas. and other issues; co-processing of cement kilns has certain technical advantages due to high temperature and long residence time, but the disposal materials are required not to affect the quality of cement, and the disposal volume is limited; plasma melting is an emerging hazardous waste disposal technology in recent years , has the advantages of complete harmlessness and obvious reduction, and basically solves the problem of secondary pollution of solid substances, but there are also problems such as the complexity of the flue gas treatment system, which is easy to cause secondary pollution, and high disposal costs.

The most important thing to achieve harmless after solid waste disposal is to solve the harmless problem of solid phase slag and gas phase after disposal. Due to the presence of harmful substances such as heavy metals in solid phase slag, making it vitrified is an important way to achieve harmlessness. Harmful substances in the gas phase mainly include NO _x , SO ₂ , HCl, H ₂ S and organic matter such as dioxin, fly ash containing heavy metals, etc. The best way to eliminate gas phase pollution is to avoid generation during the disposal process, followed by Capture by purification means to avoid discharge into the environment. The technical solutions disclosed in Chinese patents CN104053949B and CN105605581B have basically realized the problem of vitrification of solid phase slag, but due to the existence of medium and low temperature pyrolysis, there is still the problem of incomplete gas phase treatment and easy generation of tar substances. The technical scheme disclosed in Chinese patent application CN109210541A solves the problem of vitrification of solid phase slag and basically solves the problem of tars, but the content of effective gas in the synthesis gas is low, and because the gasification temperature is low (900-1000 ℃), especially in the case of fluctuating furnace conditions, there is still the problem of incomplete decomposition of some toxic organic substances.

Contents of the invention

One purpose of this application is to make the products produced by the disposal of carbonaceous materials clean and harmless.

According to one aspect of the embodiments of the present application, a two-stage melter-gasifier for the harmless disposal of carbonaceous materials is provided, the furnace includes a fluidly connected horizontal reaction section and a vertical reaction section, and the vertical reaction section is located at The horizontal reaction section is above and connected with the horizontal reaction section through an interface. The horizontal reaction section includes a low-carbon slag section, a high-carbon slag section, and a gas-phase reaction section from bottom to top, and the vertical reaction section includes a cooling reduction section. The low-carbon slag section includes a first gasification agent inlet, a first slag-supporting gas inlet, a second slag-supporting gas inlet and a liquid slag discharge outlet. The pyrolytic carbon particles in the slag section are cohesive or flowable because the carbon content is below a threshold. The high-carbon slag section includes a second gasification agent inlet, and under normal operating conditions, the pyrolytic carbon particles falling into the high-carbon slag section are not cohesive because the carbon content is higher than the threshold or mobility. The gas-phase reaction section includes a carbon-containing material inlet, a third gasification agent inlet, and a carbon-containing fine powder inlet. Under normal operating conditions, the carbon-containing material sent into the gas-phase reaction section undergoes pyrolysis, and the pyrolyzed Oxidation-reduction reactions occur in part of the products, and the generated gas phase enters the temperature-lowering reduction section through the connecting port. The temperature-lowering reduction section includes a cooling device configured to reduce the temperature inside the section, and a high-temperature crude synthesis gas outlet. Under normal operating conditions, CO2, H2O and gas containing The carbon in carbon fly ash undergoes a reduction reaction to produce CO and H2.

According to some embodiments, the first gasification agent inlet, the second gasification agent inlet and the third gasification agent inlet are configured to inject pure oxygen or oxygen-enriched air and are all provided with a flow regulating device These flow regulating devices can adjust the injection amount of the first, second and third gasification agents according to the content of CO2 in the gas discharged from the high-temperature crude synthesis gas outlet, the slag discharge temperature and the temperature in the furnace.

According to some embodiments, the first slag assisted gas inlet and the second slag assisted gas inlet are configured to inject assisted gas or inert gas, and are provided with a flow regulating device, which can The amount of combustion-supporting gas or inert gas injected is adjusted according to the condition of slag and the temperature in the furnace.

According to some embodiments, the carbonaceous material inlet is in communication with a continuous feeding device configured to continuously feed carbonaceous material into the gas phase reaction section through the carbonaceous material inlet.

According to some embodiments, the carbon-containing fine powder inlet is configured to inject carbon-containing fine powder and is provided with a flow regulating device, and the flow regulating device can be based on the content of CO2 in the gas discharged from the high-temperature raw syngas outlet and the The inlet temperature of the cooling reduction section is used to adjust the injection amount of carbon-containing fine powder.

According to some embodiments, the cooling device includes a cooling medium injection port configured to inject cooling medium into the inner space of the temperature reduction reduction section and/or a circulating cooling system provided in the furnace wall of the temperature reduction reduction section. system.

According to some embodiments, the axis of the horizontal reaction section extends approximately horizontally, the axis of the vertical reaction section extends approximately vertically, and wherein the horizontal reaction section includes a first longitudinal end and a second longitudinal end. At the longitudinal end, the carbonaceous material inlet and the connecting port are respectively located at the first longitudinal end and the second longitudinal end.

According to some embodiments, the first slag-supporting gas inlet is located at the first longitudinal end, and the second slag-supporting gas inlet is located at the second longitudinal end and is disposed near the liquid slag discharge port.

According to some embodiments, the second gasification agent inlet is located at the first longitudinal end and above the first slag-assisted gas inlet.

According to some embodiments, the third gasification agent inlet and the carbon-containing fine powder inlet are located at the second longitudinal end and are arranged near the connecting port.

According to some embodiments, the number of the first gasifying agent inlets is at least two, and they are distributed over the entire length of the horizontal reaction section at intervals.

According to another aspect of the embodiments of the present application, there is provided a method for melting and gasifying carbonaceous materials using the aforementioned two-stage melter-gasifier, comprising the following steps:

- The carbonaceous material is continuously fed into the gas phase reaction section through the carbonaceous material inlet, and the third gasification agent and carbonaceous fine powder are sprayed into the third gasification agent inlet and the carbonaceous fine powder inlet respectively. Pyrolysis of carbon-containing materials to generate pyrolysis gas, pyrolysis carbon, and carbon-containing fly ash. Pyrolysis gas and carbon-containing fly ash react quickly with the third gasification agent and carbon-containing fine powder to generate CO, CO2, H2 and H2O-based small molecular gases, entraining carbon-containing fly ash and possible residual macromolecular organic matter enter the cooling and reducing section through the connecting port, and the pyrolytic carbon falls into the high-carbon slag under the action of gravity part;

- CO2 and H2O in the gas entering the cooling reduction section from the gas phase reaction section and the carbon in the carbon-containing fly ash undergo a reduction reaction to generate CO and H2, and the possible residual macromolecular organic matter continues to decompose;

- Spray a second gasification agent into the high-carbon slag section through the second gasification agent inlet, and the second gasification agent blows away and stirs the falling pyrolytic charcoal to decompose and break up and generate heat release Oxidation-reduction reaction, the generated high-temperature gas entrains the carbon-containing fly ash produced by crushing into the gas phase reaction section, and at the same time, the pyrolytic carbon becomes low-carbon molten slag and falls to the low-carbon molten slag as the carbon content in it continues to decrease. slag section; and

- Spray a first gasification agent into the low-carbon slag section through the first gasification agent inlet, the first gasification agent stirs the slag and reacts with combustible substances in the slag to release heat, further reducing the melting The residual carbon in the slag is homogeneously vitrified, and the vitrified slag is discharged from the slag discharge port.

According to some embodiments, the step of pretreating the carbonaceous material is further included before the step of feeding the carbonaceous material, and the pretreated carbonaceous material meets the homogenization requirement.

According to some embodiments, the following steps are further included before the step of feeding carbonaceous materials: putting slag-producing materials into the melter-gasifier, passing through the first slag-supporting gas inlet, the second slag The slag-supporting gas inlet and the first gasifying agent inlet are sprayed into the first slag-supporting gas, the second slag-supporting gas and the first gasification agent, so that the first slag-supporting gas and the second slag-supporting gas Combustion reaction with the first gasification agent, heating and melting the slagging material until a stable molten pool is established, each section in the furnace reaches the predetermined temperature, and the slagging conditions are met.

According to some embodiments, the method further includes the following steps: by adjusting the amount of the second slag-supporting gas or inert gas injected from the second slag-supporting gas inlet and the amount of the inert gas injected from the first gasification agent inlet The amount of the first gasifying agent is such that the temperature of the low-carbon slag section is at least 50°C to 200°C higher than the melting point of ash under normal operating conditions.

According to some embodiments, under normal operating conditions, the temperature in the high-carbon slag section is 1350°C to 2500°C, the temperature in the gas phase reaction section is 1250°C to 2500°C, and the temperature in the cooling reduction section is The inlet temperature is from 1150°C to 2500°C.

According to some embodiments, the cooling device includes a cooling medium injection port configured to inject cooling medium into the inner space of the temperature reduction reduction section and/or a circulating cooling system provided in the furnace wall of the temperature reduction reduction section. system, by adjusting the cooling device so that the outlet temperature of the cooling reduction section is lower than the deformation temperature of the ash under normal operating conditions.

According to some embodiments, the carbonaceous fines have a particle size of less than 200 microns, preferably less than 100 microns.

According to some embodiments, the first gasification agent, the second gasification agent and the third gasification agent are all pure oxygen or oxygen-enriched air.

According to some embodiments, the total molar ratio of carbon to oxygen in the furnace materials is 0.9 to 1.3, preferably 0.95 to 1.2, and more preferably 1, by adjusting the amounts of various furnace materials.

According to some embodiments, the speed at which the second gasification agent is injected into the high-carbon slag section through the second gasification agent inlet exceeds 80 m/s.

In this application, the term "melter-gasifier" refers to a furnace for combusting and gasifying combustibles in materials fed therein and heating and melting ash and non-combustibles.

In this application, the term "carbonaceous materials" refers to materials that at least partially include carbonaceous combustibles, such as coal, petroleum, coke, biomass, plastics, rubber, domestic garbage, medical residues, oil sludge, etc.

In this application, the term "cohesiveness" means that the particles have a tendency to agglomerate and grow and adhere to each other with the slag.

In this application, the term "flowability" means that the particles have become liquid, merged with the slag, and can flow like a liquid, but the carbon content in it is still higher than 1% and does not constitute a qualified slag .

In this application, the term "pure oxygen" refers to a gas with a volume content of oxygen greater than or equal to 90%, and "oxygen-enriched air" refers to air with a volume content of oxygen greater than or equal to 22%.

In this application, the term "homogenization requirements" refers to the characteristic indicators (such as calorific value, ash composition, content amount of water) varies by no more than 6%, more preferably no more than 3%.

In this application, the term "slag-producing material" refers to the material put into the melter-gasifier to help establish a stable molten pool before the melter-gasifier enters normal operating conditions, including but not limited to coke, firewood, coal, and ash.

It is to be understood that both the foregoing general description and the following detailed description are exemplary and explanatory only and are not restrictive of the invention. Other features, objects and advantages of the invention will be apparent from the description, drawings and claims.

Description of drawings

In order to more clearly illustrate the technical solutions in the embodiments of the present application, the following briefly introduces the drawings that need to be used in the description of the embodiments. Apparently, the drawings in the following description only show some embodiments of the present invention, and those skilled in the art can also obtain other drawings according to these drawings without any creative effort.

Fig. 1 is a schematic structural view of a two-stage melter-gasifier according to some embodiments of the present application.

Fig. 2 is a flowchart of a method for melting and gasifying carbonaceous materials according to some embodiments of the present application.

Detailed ways

Reference will now be made in detail to the exemplary embodiments, examples of which are illustrated in the accompanying drawings. When the following description refers to the accompanying drawings, the same numerals in different drawings refer to the same or similar elements unless otherwise indicated. Embodiments described in the following exemplary embodiments do not represent all embodiments consistent with the present application. Rather, they are merely examples of means consistent with aspects of the present application as recited in the appended claims.

The terminology used in this application is for the purpose of describing particular embodiments only, and is not intended to limit the application. As used in this application and the appended claims, the singular forms "a", "the", and "the" are intended to include the plural forms as well, unless the context clearly dictates otherwise. It should also be understood that the term "and/or" as used herein refers to and includes any and all possible combinations of one or more of the associated listed items. "Includes" or "comprises" and similar terms mean that the elements or items listed before "comprises" or "comprises" include the elements or items listed after "comprises" or "comprises" and their equivalents, and do not exclude other elements or objects. Words such as "connected" or "connected" are not limited to physical or mechanical connections, and may include electrical connections, whether direct or indirect. "Multiple" includes two, equivalent to at least two. It should be understood that although the terms first, second, third, etc. may be used in the present invention to describe various information, the information should not be limited to these terms. These terms are only used to distinguish information of the same type from one another. For example, without departing from the scope of the present invention, first information may also be called second information, and similarly, second information may also be called first information.

A two-stage melter-gasifier 100 according to an embodiment of the present application will be described below with reference to FIG. 1 , which schematically shows the structure of the furnace. The melter gasifier is used for harmless disposal of various carbon-containing materials, especially carbon-containing waste. The melter-gasifier includes a fluidly connected horizontal reaction section 100A and a vertical reaction section 100B. The vertical reaction section 100B is located above the horizontal reaction section 100A and connected to the horizontal reaction section 100A through a joint E. The horizontal reaction section 100A includes a low-carbon slag section A, a high-carbon slag section B, and a gas phase reaction section C from bottom to top, and the vertical reaction section 100B includes a cooling reduction section D. The low-carbon slag section A includes first gasification agent inlets 121 , 122 , 123 , a first slag-supporting gas inlet 1 , a second slag-supporting gas inlet 11 and a liquid slag discharge port 10 . Under normal operating conditions, the pyrolytic carbon particles falling into the low-carbon slag section A have cohesiveness or flowability because the carbon content is lower than a threshold. The high-carbon slag section B includes a second gasification agent inlet 2 . Under normal operating conditions, the pyrolytic carbon particles falling into the high-carbon slag section B are not cohesive or flowable because the carbon content is higher than the threshold value. The threshold depends on the specific composition of the material to be treated and is usually between 10 wt% and 35 wt%. The gas phase reaction section C includes a carbonaceous material inlet 3 , a third gasification agent inlet 9 , and a carbonaceous fine powder inlet 8 . Under normal operating conditions, the carbonaceous material sent to the gas phase reaction section C is pyrolyzed during the falling process, and part of the pyrolyzed products undergo redox reactions, and the generated gas phase enters the cooling reduction section D through the connecting port E. The temperature-lowering reduction section D includes a cooling device for lowering the temperature inside this section, and a high-temperature crude synthesis gas outlet 6 . Under normal operating conditions, CO ₂ , H ₂ O in the gas entering the cooling reduction section D and carbon in the carbon-containing fly ash undergo a reduction reaction to generate CO and H ₂ .

In the melting and gasification furnace mentioned above, the carbonaceous material fed into the furnace can be Finally, it will be transformed into vitrified liquid slag and CO and _H2 -based gas phase products that do not contain macromolecular organic substances, so as to meet the requirements of cleanliness and harmlessness. In addition, since the vitrified slag has a high density and can be used as a building material, reduction and resource utilization are achieved. Moreover, the residual carbon content in the slag discharged from the above-mentioned melter-gasifier can reach an extremely low level, such as less than 1%, so that a high carbon conversion rate can be achieved, that is, a high rate of carbon in the carbonaceous material is converted into CO , CO ₂ and other small molecule carbon-containing gases. In addition, for common carbon-containing materials, the volume content of effective gas (CO and H ₂ ) in the gas phase product can reach more than 80% after being processed by the melter-gasifier of the present application (compared with the prior art, it is greatly improved) , and does not contain macromolecular organic matter, and can be further processed conveniently and pollution-free to become industrially valuable raw material gas (CO+H ₂ ) or to further react the CO in it to generate H ₂ , which can be filled as a product for external use. Sales, thereby greatly reducing the gas emissions to the environment, realizing the reduction of emissions and the resource utilization of products.

In the embodiment shown in FIG. 1, the first gasification agent inlets 121, 122, 123, the second gasification agent inlet 2 and the third gasification agent inlet 9 are used to inject gasification agent, wherein the first gasification agent The positions of the agent inlets 121, 122, 123 are set such that they can inject gasification agents into the middle and lower parts of the molten pool. In some embodiments, the gasification agent used is a gas with an oxygen content greater than or equal to 90% by volume (hereinafter referred to as pure oxygen), such as a gas with an oxygen content of 92%, 95%, 98%, or 99%. In some other embodiments, the gasification agent used is air with a volume content of oxygen greater than or equal to 22% (hereinafter referred to as oxygen-enriched air). The use of pure oxygen or oxygen-enriched air as a gasification agent is beneficial to promote the combustion reaction of combustibles, generate high-temperature gas, quickly establish a high-temperature environment, and is conducive to increasing the effective gas content. It should be understood, however, that other gasifying agents may also be used. In the embodiment shown in Figure 1, the first gasification agent inlets 121, 122, 123, the second gasification agent inlet 2 and the third gasification agent inlet 9 are respectively provided with flow regulating devices 12101, 12201, 12301, 201 , 901, these flow regulating devices can adjust the injection amount of the first, second and third gasification agents according to the content of CO ₂ in the gas discharged from the high-temperature crude syngas outlet 6, the slagging temperature and the furnace temperature. According to a possible implementation manner, these flow regulating devices are connected in communication with a controller, and the controller receives signals from the gas composition analysis sensor and the temperature sensor and sends an instruction for regulating flow to these flow regulating devices according to the signals.

In the embodiment shown in Figure 1, the first slag-supporting gas inlet 1 and the second slag-supporting gas inlet 11 are used to inject combustion-supporting gas or inert gas, wherein the combustion-supporting gas can be any combustible gas (i.e. fuel gas), such as natural gas, liquefied petroleum gas, propane, or atomized fuel oil; the inert gas can be any gas that does not react with liquid slag, such as CO ₂ , N ₂ . As shown in Figure 1, the first slag-supporting gas inlet 1 and the second slag-supporting gas inlet 11 are provided with flow regulating devices 101 and 1101 respectively, and these flow regulating devices can adjust the combustion-supporting gas according to the slag discharge condition and the temperature in the furnace. Or the amount of injection of inert gas.

In the embodiment shown in FIG. 1 , the carbon-containing fine powder inlet 8 is used for injecting carbon-containing fine powder and is provided with a flow regulating device 801, which can control the CO ₂ in the gas discharged from the high-temperature crude synthesis gas outlet 6. The content and the inlet temperature of the cooling reduction section D are used to adjust the injection amount of carbon-containing fine powder. Advantageously, the carbonaceous fines have a particle size of less than 200 microns, preferably less than 100 microns. The carbon-containing fine powder with small particle size has a larger residual carbon surface area, so it is easier to react with CO ₂ and H ₂ O, resulting in a faster heating rate and ensuring the complete decomposition of carbon-containing materials.

In the embodiment shown in Figure 1, the cooling device of the cooling reduction section D includes a cooling medium injection port 7 for injecting cooling medium into the internal space of this section and a circulating cooling system arranged in the furnace wall of this section . The cooling medium injection port 7 and the cooling medium channel of the circulating cooling system are arranged near the high-temperature crude synthesis gas outlet 6, so as to cool down the gas near the outlet. The cooling medium injection port 7 is provided with a flow regulating device 701, which can adjust the injection amount of the cooling medium. The cooling medium injected from the cooling medium injection port 7 may be water mist, water vapor, cooled syngas, carbon dioxide gas or one or more of them reaching a predetermined temperature. Fig. 1 only shows the circulating cooling medium inlet 4 and the circulating cooling medium outlet 5 of the circulating cooling system, but those skilled in the art can understand that there are also cooling medium passages in fluid communication with the inlet 4 and the outlet 5 in the furnace wall . The circulating cooling medium can be low-temperature fluids such as water and oil. By spraying the cooling medium into the inner space of the cooling reduction section D from the cooling medium injection port 7 and allowing the circulating cooling medium to circulate in the channel in the furnace wall, the outlet temperature of the cooling reduction section D can be lower than the deformation temperature of the ash ( Different ash has different deformation temperatures, which can be measured by standard test methods. Generally, the deformation temperature of common ash is 900°C to 1200°C), so that the ash loses its viscosity and avoids sticking in the high-temperature crude syngas outlet 6 and subsequent pipelines cause blockage. This allows the melter-gasifier to run for extended periods of time without frequent shutdowns for cleaning. Because the circulating cooling system can also play the role of cooling the gas in the cooling reduction section D, it can reduce the amount of cooling medium injected from the cooling medium injection port 7. In addition, there is another advantage of setting up a circulating cooling system, that is, it can recover high-quality waste heat through the heat exchange between the circulating cooling medium and high-temperature gas, and improve the thermal efficiency of the system. It should be understood that the cooling medium injection port 7 and the circulating cooling system can replace each other, but are not necessarily provided at the same time. In some embodiments, only the cooling medium injection port 7 is provided without a circulating cooling system in the furnace wall of this section. In other embodiments it is just the opposite.

As shown in FIG. 1 , the axis of the horizontal reaction section 100A extends substantially along the horizontal direction and includes a first longitudinal end 100A1 and a second longitudinal end 100A2 in the horizontal direction, while the axis of the vertical reaction section 100B generally extends along the vertical direction. extends and connects with the horizontal reaction section 100A in a fluid communication manner through the joint E provided on the upper part of the second longitudinal end 100A2 of the horizontal reaction section 100A, and the carbonaceous material inlet 3 is located at the first longitudinal end of the horizontal reaction section 100A The upper part of the end 100A1, away from the connecting port E. In this way, the horizontal distance from the carbonaceous material inlet 3 to the connecting port E (also the gas phase product produced by the gas phase reaction section C leads to the outlet of the cooling reduction section D) is long, and the pyrolysis of the material entering from the carbonaceous material inlet 3 produces Pyrolysis gas, a small amount of macromolecular organic matter, and a small amount of tar-like substances that may be produced due to insufficient pyrolysis temperature at the inlet 3 have sufficient residence time in the high-temperature gas phase reaction section C to fully react, and reach the interface E At this time, tar substances and macromolecular organic substances have basically reacted to form small molecular substances. In addition, the liquid slag outlet 10 is located at the lower part of the second longitudinal end 100A2 of the horizontal reaction section 100A, away from the carbonaceous material inlet 3 . In this way, the horizontal distance between the carbonaceous material inlet 3 and the liquid slag discharge port 10 is long, and the pyrolytic charcoal produced by the pyrolysis of the material entering from the carbonaceous material inlet 3 has enough residence time in the furnace to fully react , so that most of the carbon is finally converted into small molecule carbon-containing gases such as CO and CO ₂ , and the residual carbon content in the slag is less than 1wt%, so as to achieve a high carbon conversion rate. In addition, in this embodiment, the first slag-supporting gas inlet 1 is located at the first longitudinal end 100A1 of the horizontal reaction section 100A, while the second slag-supporting gas inlet 11 is located at the second longitudinal end 100A2 and is arranged at the liquid slag near outlet 10. In this way, when starting the furnace, the first slag-supporting gas inlet 1 and the second slag-supporting gas inlet 11, which are located at both ends of the horizontal reaction section 100A, can be injected into the combustion-supporting gas at the same time, and through the first gasification agent inlet 121, 122 and 123 spray the first gasification agent to heat and melt the slagging material, quickly establish a stable molten pool and meet the slag discharge conditions, and make each section of the furnace reach the predetermined temperature as soon as possible to meet the conditions for normal operation. In addition, during the operation of the equipment, the slagging temperature can be adjusted by adjusting the amount of the slag-supporting gas injected from the second slag-supporting gas inlet 11 to meet different slagging requirements. How to adjust it will be introduced below. In the embodiment shown in FIG. 1 , the second gasification agent inlet 2 is located at the first longitudinal end 100A1 of the horizontal reaction section 100A and above the first slag-supporting gas inlet 1 . In this way, the pyrolytic charcoal produced by the pyrolysis of the material entering from the carbonaceous material inlet 3 at the first longitudinal end 100A1 during the falling process will be quickly injected by the gasification agent injected into the second gasification agent inlet 2 at a high speed. (and the high-temperature gas rising from the low-carbon slag section A) is blown away, further decomposed and broken, and has an exothermic reaction with the gasification agent, and the generated high-temperature gas returns to the gas phase reaction section C to provide continuous pyrolysis of carbon-containing materials. Heat supply, so that the temperature of the gas phase reaction section C always meets the requirements of pyrolysis. In addition, as shown in FIG. 1 , the third gasification agent inlet 9 and the carbon-containing fine powder inlet 8 are located at the second longitudinal end 100A2 of the horizontal reaction section 100A and are arranged near the joint E. In this way, the temperature of the gas phase that enters the cooling reduction section D through the interface E can be controlled by adjusting the amount of the third gasification agent and the carbon-containing fine powder injected from the third gasification agent inlet 9 and the carbon-containing fine powder inlet 8 , so that it meets the requirement of 1150°C or higher, and at the same time, the oxygen in the third gasification agent reacts quickly with the rising macromolecular organic matter, which is conducive to the elimination of macromolecular organic matter as soon as possible.

In the embodiment shown in FIG. 1 , the carbonaceous material inlet 3 is in communication with a continuous feeding device 302 (for example, a screw feeding device). In this way, carbonaceous materials that meet the requirements of homogenization after pretreatment (such as coal, petroleum, coke, biomass, plastics, rubber, domestic garbage, pharmaceutical residues, and oil sludge are mixed according to the indicators) It can be continuously sent to the gas-phase reaction section of the melter-gasifier to ensure that the temperature in the furnace and the composition of the high-temperature crude synthesis gas produced are stable.

It should be understood that FIG. 1 only schematically illustrates one possible configuration of a melter-gasifier according to some embodiments. In the embodiment shown in the figure, the vertical reaction section 100B of the melter-gasifier has the shape of a cylinder whose longitudinal axis extends approximately in the vertical direction, and the horizontal reaction section 100A has the shape of a cylinder whose longitudinal axis extends approximately in the horizontal direction. cylindrical shape, but it should be understood that they may also have other shapes. In some embodiments, both the horizontal reaction zone and the vertical reaction zone have a cylindrical shape with a polygonal (eg, quadrilateral, pentagonal, or hexagonal) cross-section. In some other embodiments, the vertical reaction section has a truncated circular shape with a cross-sectional area gradually changing in the vertical direction, while the horizontal reaction section is cylindrical. In yet other embodiments, some or all of the various sections of the melter-gasifier have shapes that differ from one another. And it should be understood that the above-mentioned low-carbon slag section A, high-carbon slag section B, gas-phase reaction section C, and cooling reduction section D are only a rough functional division, and there are no strict physical boundaries, and there are even gaps between adjacent sections. There is at least partial overlap. In addition, the heights and proportions of the above-mentioned sections can be determined by those skilled in the art, for example, according to the nature and quantity of the materials to be processed, which are not limited in this application.

It should also be understood that Fig. 1 only schematically shows the approximate position and quantity of each inlet and outlet, but those skilled in the art can adjust the position and quantity of each inlet and outlet according to actual needs. For example, Fig. 1 shows three first gasification agent inlets 121, 122, 123, but those skilled in the art can set more or fewer The first gasifying agent inlet. Specifically, if the horizontal reaction section 100A is very short, one or two inlets for the first gasification agent can meet the demand; if the horizontal reaction section 100A is very long, the characteristics of slag at different cross-sections will be different. Different amounts of the first gasification agent need to be injected, so it is necessary to set multiple first gasification agent inlets, for example, 4, 5 or even more, on the entire length of the horizontal reaction section 100A. For another example, although some inlets and outlets are only shown in Fig. 1, those skilled in the art can arrange multiple inlets and outlets at suitable positions according to the size of the furnace, and the inlets with different functions can even overlap, For example, the carbon-containing fine powder inlet 8 and the third gasification agent inlet 9 may be the same port, and the carbon-containing fine powder and the third gasification agent are injected into the port simultaneously by means of a pipe with double channels.

It should also be understood that although not shown in the figure, the melter-gasifier according to various embodiments of the present application may also include various sensors at appropriate positions, such as temperature sensors, gas composition analysis sensors, flow sensors, etc., for The signals are transmitted to the controller, and the controller controls the flow regulating devices at each inlet according to these signals, so that the injection amount and injection timing of various substances injected into the furnace are as optimal as possible, so that the melting and gasification The furnace is running at its best.

Referring to Fig. 1 and Fig. 2, a method for melting and gasifying carbonaceous materials by using the above-mentioned melting and gasifying furnace will be described below. Fig. 2 is a schematic flowchart of a method according to some embodiments of the present application. It should be understood that although the various steps in the flow chart of FIG. 2 are displayed sequentially as indicated by the arrows, these steps are not necessarily executed sequentially in the order indicated by the arrows. Unless otherwise specified herein, the execution of these steps is not strictly limited in order, but may be executed in other orders. Moreover, at least some of the steps in the figure may include multiple sub-steps or multiple stages, these sub-steps or stages are not necessarily executed at the same time, but may be executed at different times, and the execution order is not necessarily sequential Instead, it may be performed alternately or alternately with at least a part of other steps or sub-steps or stages of other steps.

In the embodiment shown in Figure 2, the method includes the following steps:

Step S1: The carbon-containing material is continuously sent into the gas phase reaction section C through the carbon-containing material inlet 3, and the third gasification agent and carbon-containing fine powder are sprayed into the third gasification agent inlet 9 and the carbon-containing fine powder inlet 8 respectively, Pyrolyze carbon-containing materials to generate pyrolysis gas (the composition varies with the carbon-containing materials fed in, and may include one or more of CO, H ₂ , CO ₂ , CH ₄ , H ₂ S, etc.) , pyrolytic carbon, and carbon-containing fly ash, pyrolysis gas and carbon-containing fly ash react quickly with the third gasification agent and carbon-containing fine powder to generate small molecules mainly composed of CO, CO ₂ , H ₂ and H ₂ O The gas entrains carbon-containing fly ash and possible residual macromolecular organic matter into the cooling reduction section D, and the pyrolytic carbon falls into the high-carbon slag section B under the action of gravity;

Step S2: CO ₂ , H ₂ O in the gas entering the cooling reduction section D from the gas phase reaction section C undergoes a reduction reaction with the carbon in the carbon-containing fly ash to generate CO and H ₂ , and the possible residual macromolecular organic matter continues to decompose;

Step S3: inject a second gasification agent into the high-carbon slag section B through the second gasification agent inlet 2 (preferably, the speed of injecting the second gasification agent exceeds 80m/s), and the second gasification agent Stir the falling pyrolytic carbon to make it decompose and break up and undergo exothermic oxidation-reduction reaction. The generated high-temperature gas entrains the carbon-containing fly ash produced by the crushing into the gas phase reaction section C. and become low-carbon molten slag and fall to low-carbon molten slag section A; and

Step S4: inject the first gasification agent into the low-carbon slag section A through the first gasification agent inlets 121, 122, 123, the first gasification agent stirs the slag and reacts with the combustible substances in the slag to release heat , further reduce the residual carbon in the slag and make it homogeneously vitrified, and the vitrified slag is discharged from the slag discharge port 10.

In the above method, under normal operating conditions, the gas-phase reaction section C has a high-temperature environment (in some embodiments, up to 1250°C to 2500°C), so that the carbonaceous materials fed in undergo high-temperature pyrolysis to generate pyrolysis Gas, pyrolytic carbon and carbon-containing fly ash (the temperature near the carbon-containing material inlet 3 is relatively low, and the pyrolysis here may also produce a small amount of tar-like substances and macromolecular organic substances). On the one hand, pyrolysis gas, carbon-containing fly ash, and a small amount of tar-like substances and macromolecular organic matter move to the second longitudinal end 100A2 of the horizontal reaction section 100A, and the third gas injected from the third gasification agent inlet 9 The chemical agent, a small amount of carbon-containing fine powder sprayed from the carbon-containing fine powder inlet 8, and the high-temperature gas generated in the high-carbon slag section B are quickly mixed and reacted in the high-temperature environment of the gas-phase reaction section C to generate CO, CO ₂ , H ₂ and H ₂ O-based small molecular gas, the gas entrains carbon-containing fly ash and possible residual macromolecular organic matter into the same high-temperature environment (in some embodiments, the inlet temperature of this section is 1150°C to 2500°C, the outlet temperature is lower than the deformation temperature of the ash), the cooling reduction section D, in which CO ₂ and H ₂ O react with the carbon in the carbon-containing fly ash to generate CO and H ₂ , and possibly residual macromolecules Organic matters continue to decompose into small molecular gases at high temperature, so that the residual carbon content in fly ash is greatly reduced, and the gas finally discharged from outlet 6 of high-temperature raw syngas contains more than 80% (volume ratio) of CO and H ₂ , and a small amount of CO ₂ (volume content less than 10%, less than 5% under stable conditions) and H ₂ O, a very small amount of CH ₄ , H ₂ S, N ₂ and other small molecular gases, and a small amount of fly ash, without any Macromolecular organic matter, thus effectively avoiding the production of tar substances in the process of conventional combustion and medium-low temperature pyrolysis, avoiding the production of benzene, phenols, and dioxins from the source, and realizing the harmlessness of the gas phase. Moreover, compared with the prior art, the content of effective gas (that is, CO and H ₂ ) in the gas discharged from the high-temperature crude synthesis gas outlet 6 is significantly improved, so that it can be processed afterward (not shown in the accompanying drawings of the application) Subsequent processing equipment) becomes industrially valuable raw material gas (CO+H2) or further reacts CO in it to generate _H2 , which is filled and sold as a product, realizing the resource utilization of the product. Only a very small amount of CO ₂ and H ₂ O is finally discharged into the atmosphere, thereby greatly reducing the impact on the environment. On the other hand, the pyrolytic charcoal (solid phase) generated by pyrolysis falls into the high-carbon slag section B that also has a high-temperature environment (in some embodiments, up to 1350°C to 2500°C) under the action of gravity. In the process, the pyrolytic charcoal is dispersed under the agitation of the second gasification agent injected at a high speed from the second gasification agent inlet 2, and further decomposed and broken in a high-temperature environment, and a redox reaction occurs, a large amount of heat is released, and a The high-temperature gas (mainly CO and CO ₂ , the temperature can reach 1500℃～3000℃) entrains the carbon-containing fly ash produced by crushing into the gas phase reaction section C. At the same time, the pyrolytic carbon changes with the continuous reduction of carbon content. The low-carbon molten slag falls to the low-carbon slag section A (the temperature here varies greatly, but the lowest temperature is 50°C to 200°C higher than the melting point of ash, and the highest temperature may exceed 2500°C). In the low-carbon slag section A, the pyrolytic charcoal melts into a liquid state and fuses with the slag, and the first gasification agent injected from the first gasification agent inlet 121, 122, 123 stirs the slag and combines with the slag The carbon and other combustible substances in the slag react to release heat, further reduce the residual carbon in the slag and make it homogeneously vitrified, and effectively solidify the heavy metals, thereby realizing the harmlessness of the solid slag. Also, since the vitrified slag has a high density and can be used as a building material, volume reduction and resource utilization are achieved. In addition, due to the long residence time of the solid phase in the high-temperature environment in the furnace (successively passing through the gas phase reaction section C, high-carbon slag section B, and low-carbon slag section A) and fully mixed under the agitation of the gasification agent, The reaction is complete, so most of the carbon in it is finally converted into small molecule carbon-containing gases such as CO and CO ₂ , and the residual carbon content in the slag is less than 1wt%, thus achieving a high carbon conversion rate. This can be achieved even with poorly reactive materials. In addition, due to the long residence time of ash and slag in the high-temperature environment in the furnace, the temperature field in the furnace is evenly distributed, the reaction speed is fast under the action of gas stirring, and the reaction between carbon and oxygen is sufficient, so the slag homogenization is thorough and better. Vitrification is more conducive to the solidification of heavy metals.

When the carbonaceous material to be processed does not meet the requirements, it needs to be pretreated before being put into the furnace. Therefore, in some embodiments, the above method also includes the step of pretreating the carbonaceous material, for example, after drying several different materials, they are mixed according to the index, so that the carbonaceous material after pretreatment meets the requirements of homogeneity. Chemical requirements, that is, in the process of material transportation, the change in the characteristic indicators (such as calorific value, ash composition, water content) of the material passing through a certain cross-section in the first minute and the material passing in the next minute shall not exceed 6%, which is better ground is not more than 3%. Through the pretreatment of the material, the properties of the material entering the melter-gasifier are relatively stable, and there is no need to frequently adjust the preset operating parameters of the furnace, and the furnace can run stably for a long time. In addition, through pretreatment, the melter-gasifier can also handle more kinds of carbonaceous materials, which has a wide range of application.

In the method according to the embodiment shown in Fig. 2, the S0 step is also included before the S1 step, and in the S0 step, slag-producing materials (such as coke, firewood, coal, ash, etc.) are put into the melter-gasifier, through The first slag-supporting gas inlet 1, the second slag-supporting gas inlet 11 and the first gasification agent inlets 121, 122, 123 are sprayed into the first slag-supporting gas and the second slag-supporting gas (such as natural gas, liquefied gas, etc.) Any combustible gas such as gas, propane or atomized fuel oil) and the first gasification agent (such as pure oxygen, oxygen-enriched air), so that the combustion-supporting gas and the first gasification agent undergo a combustion reaction, heating and melting to produce slag Materials until a stable molten pool is established, each section in the furnace reaches the predetermined temperature, and the conditions for slag discharge are met. Subsequently, the carbonaceous material to be disposed is sent into the furnace and a predetermined amount of corresponding substances are sprayed into the above-mentioned various inlets to cause the above-mentioned various reactions to occur. Since these reactions are mostly exothermic reactions, a large amount of Therefore, under normal operating conditions, the average temperature in the gas phase reaction section C can be maintained at 1250°C to 2500°C, the temperature in the high-carbon slag section B can be maintained at 1350°C to 2500°C, and the low-carbon slag section The temperature in A is at least 50°C to 200°C higher than the melting point of ash (the slag-supporting gas injected through the second slag-supporting gas inlet 11 is used to adjust the slag discharge temperature), and the inlet temperature of the cooling reduction section D is 1150°C To 2500°C, the outlet temperature is lower than the deformation temperature of the ash (achieved by the cooling device). Generally, during normal operation, it is only necessary to inject a small amount of the first and second oxidizing gases or pass in an inert gas to keep the orifice unblocked. When it is necessary to increase the amount of slag discharge or slag plugging, the amount of the second combustion-supporting gas injected from the second slag-supporting gas inlet 11 can be appropriately increased so that it can reach a suitable stoichiometric ratio with the first gasification agent (such as complete combustion stoichiometric ratio), thereby increasing the slagging temperature. When it is necessary to reduce or not discharge slag, the amount of the second oxidizing gas injected from the second slag-supporting gas inlet 11 can be reduced or the second oxidizing gas can be switched to an inert gas, and it is sufficient to keep the inlet unblocked. In addition, when the calorific value of the carbonaceous material fed into the melter-gasifier is low or the temperature in the furnace fluctuates so that the temperature cannot meet the requirements, it can be increased by increasing the gas-supporting inlet 1 from the first slag, the second slag The amount of the supporting gas injected into the supporting gas inlet 11 ensures the high temperature environment in the furnace.

In some embodiments, the above method further includes the following steps: by adjusting the amount of various materials entering the furnace (that is, all materials entering the furnace, including combustion-supporting gas, gasification agent, carbon-containing materials, and carbon-containing fine powder), the input The total molar ratio of carbon to oxygen in the furnace charge is 0.9 to 1.3, preferably 0.95 to 1.2, more preferably 1. In this way, a higher cooling efficiency (that is, the ratio of the calorific value of the effective gas produced by the same amount of materials fed into the furnace to the heat value of the materials fed into the furnace) can be obtained, and the economy is improved.

The effects achieved by the present application will be described below by taking a melter-gasifier according to some embodiments as an example.

Example 1: A melter-gasifier capable of handling 240 tons of solid material per day, wherein the inner diameter of the horizontal reaction section is 2200 mm, the length is 4500 mm, the inner diameter of the vertical reaction section is 2800 mm, and the height is 6500 mm. The materials fed into the furnace It is a mixture of pretreated domestic waste and tar residue, with a calorific value of 25634Kj/kg, and the specific components are shown in Table 1:

Table 1

Into the furnace composition (including combustion gas)	mass percentage
moisture	8
Ash	18
C	61.46
h	3.56
o	7.21
S	0.9
N	0.87

The main operating parameters and the parameters of the final product when the melter-gasifier handles the above-mentioned materials are as shown in Table 2:

Table 2

project	unit	value
Vaporization temperature	℃	1350
Furnace material volume	t/h	10
Furnace oxygen	Nm 3 /h	5140

Syngas flow	Nm 3 /h	18109
Effective gas (CO+H 2 ) flow rate	Nm 3 /h	16601
steam production	t/h	15
carbon conversion rate	%	99.9
Solid slag contains carbon	% (mass ratio)	<0.5%
CO	%(Volume ratio)	68.28
H 2	%(Volume ratio)	23.39
CO 2	%(Volume ratio)	3.05
H 2 O	%(Volume ratio)	3.29
CH 4	ppm (volume ratio)	3525.7
H 2 S	%(Volume ratio)	0.31
N 2	%(Volume ratio)	1.32

From the above data, it can be seen that in this example, the high-temperature crude syngas generated after the carbonaceous material is _processed by the melter-gasifier does not contain any macromolecular organic matter, and the effective gas (CO and H ₂ ) content is as high as 94.79%, the thermal efficiency of the by-product steam is high, the solid slag contains low carbon and is glass body, which realizes the requirement of harmless disposal of solid waste, that is, solves the problem of harmless solid phase slag and gas phase after disposal problem.

Example 2: A melting gasifier capable of processing 360 tons of solid material per day, wherein the inner diameter of the horizontal reaction section is 2400mm, the length is 6000mm, the inner diameter of the vertical reaction section is 3000mm, and the height is 8000mm, the materials sent into the furnace It is pretreated domestic waste with a calorific value of 20285Kj/kg, and its specific composition is shown in Table 3:

table 3

Into the furnace composition (including combustion gas)	mass percentage
moisture	5
Ash	25
C	54

h	2.55
o	12.16
S	0.32
N	0.97

The main operating parameters and the parameters of the final product when the melter-gasifier handles the above-mentioned materials are as shown in Table 4:

Table 4

project	unit	value
Vaporization temperature	℃	1350
Furnace material volume	t/h	15
Furnace oxygen	Nm 3 /h	6570
Syngas flow	Nm 3 /h	23565
Effective gas (CO+H 2 ) flow rate	Nm 3 /h	18975
steam production	t/h	20
carbon conversion rate	%	99.9
Solid slag contains carbon	the	<0.5%
CO	%(Volume ratio)	62.38
H 2	%(Volume ratio)	18.13
CO 2	%(Volume ratio)	8.15
H 2 O	%(Volume ratio)	7.47
CH 4	ppm (volume ratio)	661.49
H 2 S	%(Volume ratio)	0.12
N 2	%(Volume ratio)	3.68

From the above data, it can be seen that in this example, the high-temperature crude syngas generated after the carbonaceous material is _processed by the melter-gasifier does not contain any macromolecular organic matter, and the effective gas (CO and H ₂ ) content is as high as 87.01%, the thermal efficiency of the by-product steam is high, the solid slag contains low carbon and is glass body, which realizes the requirement of harmless disposal of solid waste, that is, solves the problem of harmless solid phase slag and gas phase after disposal problem.

In summary, the melter-gasifier and the method for harmless disposal of carbonaceous materials provided by the embodiment of the present application have many advantages and broad application prospects, especially the harmless disposal process can be realized. , material reduction and resource utilization.

The drawings and above description describe specific non-limiting embodiments of the present application. In order to teach inventive principles, some conventional aspects have been simplified or omitted. Those skilled in the art should understand that any modifications, equivalent replacements, improvements, etc. made within the spirit and principles of the present application shall be included in the protection scope of the present application. Those skilled in the art should understand that the above-mentioned features can be combined in various ways without conflicting conditions to form multiple variations of the present application. As a result, the invention is not limited to the particular embodiments described above, but only by the claims and their equivalents.

Claims (21)

1. A two-stage melter-gasifier (100) for harmlessly disposing of carbonaceous materials, characterized in that the melter-gasifier includes a fluidly connected horizontal reaction section (100A) and a vertical reaction section (100B), The vertical reaction section is located above the horizontal reaction section and is connected to the horizontal reaction section through an interface (E), wherein the horizontal reaction section includes a low-carbon slag section ( A), high-carbon slag section (B), gas phase reaction section (C), the vertical reaction section includes a cooling reduction section (D),

   Wherein, the low-carbon slag section (A) includes the first gasification agent inlet (121, 122, 123), the first slag-supporting gas inlet (1), the second slag-supporting gas inlet (11) and liquid The slag outlet (10), under normal operating conditions, the pyrolytic carbon particles falling into the low-carbon slag section have cohesiveness or flowability because the carbon content is lower than a threshold;

   Wherein, the high-carbon slag section (B) includes a second gasification agent inlet (2), and under normal operating conditions, pyrolytic carbon particles falling into the high-carbon slag section have a carbon content higher than the above threshold without being cohesive or flowable;

   Wherein, the gas-phase reaction section (C) includes a carbon-containing material inlet (3), a third gasification agent inlet (9), and a carbon-containing fine powder inlet (8). The carbon-containing material in the gas phase reaction section undergoes pyrolysis, and some pyrolyzed products undergo redox reactions, and the gas phase generated enters the cooling reduction section (D) through the connecting port (E); and

   Wherein, the temperature reduction reduction section (D) includes a cooling device configured to reduce the temperature inside the section, and a high-temperature crude synthesis gas outlet (6). Under normal operating conditions, the gas entering the temperature reduction reduction section CO ₂ , H ₂ O in the gas and carbon in the carbon-containing fly ash undergo a reduction reaction to generate CO and H ₂ .
2. The two-stage melter-gasifier according to the preceding claim, wherein the first gasification agent inlet (121, 122, 123), the second gasification agent inlet (2) and the third The gasifying agent inlet (9) is configured to inject pure oxygen or oxygen-enriched air and is provided with flow regulating devices (12101, 12201, 12301, 201, 901), and these flow regulating devices can The content of _CO2 in the gas discharged from the outlet (6), the slagging temperature and the temperature in the furnace are used to adjust the injection amount of the first, second and third gasification agents.
3. The two-stage melter-gasifier according to any one of the preceding claims, wherein the first slag-assisted gas inlet (1) and the second slag-assisted gas inlet (11) are configured for Combustion-supporting gas or inert gas is injected, and a flow regulating device (101, 1101) is provided, and the flow-regulating device can adjust the injection amount of combustion-supporting gas or inert gas according to the slagging condition and the temperature in the furnace.
4. The two-stage melter-gasifier according to any one of the preceding claims, wherein the carbonaceous material inlet (3) communicates with a continuous feeding device (302), and the continuous feeding device (302) is configured as It is used to continuously feed carbonaceous material into the gas phase reaction section (C) through the carbonaceous material inlet (3).
5. The two-stage melter-gasifier according to any one of the preceding claims, wherein the carbon-containing fine powder inlet (8) is configured to inject carbon-containing fine powder and is provided with a flow regulating device (801) , the flow regulating device can adjust the injection amount of carbon-containing fine powder according to the content of _CO2 in the gas discharged from the high-temperature crude synthesis gas outlet (6) and the inlet temperature of the cooling reduction section.
6. The two-stage melter-gasifier according to any one of the preceding claims, wherein the cooling device includes a cooling medium injection port ( 7) and/or a circulating cooling system arranged in the furnace wall of the temperature reduction reduction section.
7. The two-stage melter-gasifier according to any one of the preceding claims, wherein the axis of the horizontal reaction section (100A) extends substantially along the horizontal direction, and the axis of the vertical reaction section (100B) extends approximately Extending in the vertical direction, and wherein, the horizontal reaction section (100A) includes a first longitudinal end (100A1) and a second longitudinal end (100A2), the carbonaceous material inlet (3) is connected to the interface ( E) at said first longitudinal end and said second longitudinal end, respectively.
8. The two-stage melter-gasifier according to the preceding claim, wherein the first slag-assisted gas inlet (1) is located at the first longitudinal end, and the second slag-assisted gas inlet (11) It is located at the second longitudinal end and is arranged near the liquid slag discharge port (10).
9. The two-stage melter-gasifier according to any one of claims 7-8, wherein the second gasification agent inlet (2) is located at the first longitudinal end (100A1) and at the first Above the slag-supporting gas inlet (1).
10. The two-stage melter-gasifier according to any one of claims 7-9, wherein the third gasification agent inlet (9) and the carbon-containing fine powder inlet (8) are located in the second The longitudinal end is arranged near the said joint (E).
11. The two-stage melter-gasifier according to any one of the preceding claims, wherein the number of the first gasification agent inlets (121, 122, 123) is at least two, and are distributed at intervals between each other. On the whole length of above-mentioned horizontal reaction section (100A).
12. A method for melting and gasifying carbonaceous materials using a two-stage melter-gasifier (100) as claimed in any one of the preceding claims, comprising the following steps:

    - the carbonaceous material is continuously fed into the gas phase reaction section (C) through the carbonaceous material inlet (3) and passed through the third gasification agent inlet (9) and the carbonaceous fine powder inlet (8) Spray the third gasification agent and carbon-containing fine powder respectively to pyrolyze the carbon-containing material to generate pyrolysis gas, pyrolysis carbon, and carbon-containing fly ash. The pyrolysis gas and carbon-containing fly ash are combined with the third gasification The agent and carbon-containing fine powder quickly react to generate small molecule gases mainly CO, CO ₂ , H ₂ and H ₂ O, and entrain carbon-containing fly ash and possible residual macromolecular organic matter to enter the all through the interface (E). The cooling reduction section (D), pyrolytic carbon falls into the high-carbon slag section (B) under the action of gravity;

    - CO _{2 ,} H ₂ O in the gas entering the cooling reduction section (D) from the gas phase reaction section (C) undergoes a reduction reaction with carbon in carbon-containing fly ash to generate CO and H ₂ , and the remaining Macromolecular organic matter continues to decompose;

    - Spraying a second gasification agent into the high-carbon slag section (B) through the second gasification agent inlet (2), the second gasification agent blows away and agitates the falling pyrolytic char to decompose it Broken and an exothermic redox reaction occurs, the generated high-temperature gas entrains the carbon-containing fly ash produced by the crushing into the gas phase reaction section (C), and at the same time, the pyrolytic carbon becomes low-carbon as the carbon content in it continues to decrease Molten slag falls to said low-carbon slag section (A); and

    - Spray a first gasification agent into the low-carbon slag section (A) through the first gasification agent inlet (121, 122, 123), the first gasification agent stirs the slag and mixes with the slag The combustible substances react to release heat, further reduce the carbon residue in the slag and make it homogeneously vitrified, and the vitrified slag is discharged from the slag discharge port (10).
13. The method according to claim 12, wherein, before the step of feeding the carbonaceous material, it further includes the step of pretreating the carbonaceous material, and the pretreated carbonaceous material meets the homogenization requirement.
14. The method according to any one of claims 12-13, wherein, before the step of feeding carbonaceous materials, the following steps are further included: putting slag-producing materials into the melter-gasifier, passing through the first A slag-supporting gas inlet (1), the second slag-supporting gas inlet (11) and the first gasification agent inlet (121, 122, 123) are respectively injected into the first slag-supporting gas, the second The slag-supporting gas and the first gasification agent make the first slag-supporting gas, the second slag-supporting gas and the first gasification agent undergo a combustion reaction, and heat and melt the slag-producing material until a stable molten pool is established and each section in the furnace Reach the predetermined temperature and meet the conditions for slag discharge.
15. The method according to any one of claims 12-14, further comprising the steps of: adjusting the amount of the second slag-supporting gas or inert gas injected from the second slag-supporting gas inlet (1) and The amount of the first gasification agent injected from the first gasification agent inlet (121, 122, 123) makes the temperature of the low-carbon slag section (A) at least higher than that of the ash under normal operating conditions. Melting point 50°C to 200°C.
16. The method according to any one of claims 12-15, wherein, under normal operating conditions, the temperature in the high-carbon slag section (B) is 1350°C to 2500°C, and the gas phase reaction section ( The temperature in C) is from 1250°C to 2500°C, and the inlet temperature of the temperature reduction reduction section (D) is from 1150°C to 2500°C.
17. The method according to any one of claims 12-16, wherein the cooling device comprises a cooling medium injection port (7) configured to inject a cooling medium into the internal space of the cooling reduction section and/or Or the circulating cooling system installed in the furnace wall of the cooling reduction section, by adjusting the cooling device, the outlet temperature of the cooling reduction section under normal operating conditions is lower than the deformation temperature of ash.
18. A method according to any one of claims 12-17, wherein the carbonaceous fines have a particle size of less than 200 microns, preferably less than 100 microns.
19. The method according to any one of claims 12-18, wherein the first gasification agent, the second gasification agent and the third gasification agent are all pure oxygen or oxygen-enriched air.
20. The method according to any one of claims 12-19, wherein, by adjusting the amount of various furnace materials, the total molar ratio of carbon and oxygen in the furnace materials is 0.9 to 1.3, preferably 0.95 to 1.2, More preferably 1.
21. The method according to any one of claims 12-20, wherein the speed at which the second gasification agent is injected into the high-carbon slag section (B) through the second gasification agent inlet (2) exceeds 80m/s.

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