阅读说明：本技术 一种固定床气化炉及排灰排渣方法 (Fixed bed gasification furnace and ash and slag discharging method ) 是由 李冶 于 2021-03-05 设计创作，主要内容包括：本发明公开了一种固定床气化炉及排灰排渣方法,包括炉体,所述炉体的上端通过导料管连接有高压料仓,炉体上部设有出气口,炉体上部内部中设有测温管,测温管内部设有若干个不同高度位置的用于测量温度的热电偶,炉体的锥形下部炉体下部设有固体料排出区,炉体下部设有至少两组助剂进口,固体料排出料区的出口端连接有残碳处理机构。本发明将气化炉反应气体的布风结构和排灰结构显著地简化,可直接进行干法排灰控制,在需要进入熔渣操作范围时,将残碳燃烧和灰渣熔融的过程从气化炉本体上分离出来,采用小型的燃烧装备完成灰渣熔融操作,气化炉排灰排渣得到精准控制,且气化炉的启停热备等操作变得更简易,明显有利于提高固定床气化炉的可靠性和可用性,实现固体渣和液态渣的排放。(The invention discloses a fixed bed gasification furnace and an ash and slag discharging method, comprising a furnace body, wherein the upper end of the furnace body is connected with a high-pressure bin through a material guide pipe, the upper part of the furnace body is provided with an air outlet, a temperature measuring pipe is arranged in the upper part of the furnace body, a plurality of thermocouples for measuring temperature are arranged in the temperature measuring pipe at different height positions, the lower part of the furnace body at the conical lower part of the furnace body is provided with a solid material discharging area, the lower part of the furnace body is provided with at least two groups of auxiliary agent inlets, and the outlet end of the solid. The invention obviously simplifies the air distribution structure and the ash discharge structure of the reaction gas of the gasification furnace, can directly carry out dry ash discharge control, separates the processes of carbon residue combustion and ash slag melting from the gasification furnace body when the operation range of slag needs to be entered, adopts small combustion equipment to complete the ash slag melting operation, accurately controls the ash discharge and the ash discharge of the gasification furnace, simplifies the operations of starting, stopping, heat preparation and the like of the gasification furnace, is obviously beneficial to improving the reliability and the availability of the fixed bed gasification furnace, and realizes the discharge of solid slag and liquid slag.)

1. The utility model provides a fixed bed gasifier, includes the furnace body, its characterized in that, the upper end of furnace body is connected with high-pressure feed bin through the passage, and furnace body upper portion is equipped with the gas outlet, is equipped with the temperature measurement pipe in the furnace body upper portion is inside, and the temperature measurement inside is equipped with the thermocouple that is used for measuring temperature of a plurality of different altitude positions, and the furnace body lower part is equipped with solid material exhaust area, and the furnace body lower part is equipped with at least two sets of auxiliary agent import, and the exit end of solid material exhaust area is connected with.

2. The fixed bed gasification furnace according to claim 1, wherein the residual carbon treatment means comprises a residual carbon cyclone combustion cylinder and a slag quenching cylinder which are connected, the residual carbon cyclone combustion cylinder is provided with an auxiliary agent introduction port, the lower portion of the furnace body is formed into a conical shape, and the conical lower portion of the furnace body is provided with a control valve which is connected with the residual carbon cyclone combustion cylinder.

3. The fixed bed gasification furnace according to claim 2, wherein the carbon residue cyclone combustion cylinder and the slag quenching cylinder are both vertically arranged, and an inlet end of the carbon residue cyclone combustion cylinder is connected with the solid material discharge area.

4. A fixed-bed gasification furnace according to claim 2, wherein a discharge controller is provided in the solid material discharge zone.

5. The fixed bed gasification furnace according to claim 4, wherein the carbon residue cyclone combustion cylinder is inclined with a higher end and a lower end, the slag quenching cylinder is arranged vertically, the control valve is connected to a feeding end of the carbon residue cyclone combustion cylinder, the flue gas return pipe is connected to a side wall of the carbon residue cyclone combustion cylinder, and an inlet end of the carbon residue cyclone combustion cylinder is connected to the solid material discharge area.

6. The fixed bed gasification furnace according to claim 4, wherein the carbon residue cyclone combustion cylinder and the slag quenching cylinder are both vertically arranged, the control valve is connected to a side wall of the carbon residue cyclone combustion cylinder, the solid material discharge area is connected to a side wall of the carbon residue cyclone combustion cylinder, and the flue gas return pipe is connected to an inlet end of the carbon residue cyclone combustion cylinder.

7. The fixed-bed gasification furnace according to claim 1, wherein a slag pot is attached to an outlet end of the fixed material discharge zone.

8. The fixed bed gasification furnace according to claim 1, wherein the carbon residue treatment mechanism comprises an ash melting control cylinder and a slag quencher, the ash melting control cylinder is connected with the outlet end of the solid material discharge area, the bottom of the ash melting control cylinder is provided with a pneumatic valve, the ash melting control cylinder is provided with an auxiliary agent inlet, the slag quencher is provided with a balance pipe, the balance pipe is provided with a discharge port, the slag quencher is provided with make-up gas above, the pneumatic valve extends obliquely from bottom to top, the high end of the pneumatic valve is connected with the inlet of the slag quench port, the low end of the pneumatic valve is connected with the ash melting control cylinder, and the difference between the height position of the high end and the low end of the pneumatic valve is larger than the pipe diameter of the pneumatic valve.

9. The fixed bed gasification furnace according to claim 2, wherein a baffle plate is arranged in the lower part of the furnace body and is positioned above the connecting position of the carbon residue cyclone combustion cylinder and the furnace body, the lower part of the furnace body is in a cone shape, an auxiliary agent introducing port or an auxiliary agent inlet is internally provided with an auxiliary inner air distribution assembly so that the auxiliary agent uniformly enters the furnace body, and the auxiliary agent introducing port or the auxiliary agent inlet is used for introducing oxygen and water vapor.

10. The ash discharge and slag discharge method of the fixed bed gasification furnace is characterized by comprising the following steps of:

before starting, filling a part of ash and slag into the bottom of the gasification furnace, filling the ash and slag into the fixed material discharge area, then pre-filling crushed coal on the ash and slag layer to reach the normal material level of the gasification furnace, and filling a high-pressure material bin with the crushed coal through a coal lock for standby;

when the gasification furnace is started, inputting a plurality of paths of mixed gas of oxygen and water vapor from the lower part of the gasification furnace, wherein the proportions of the oxygen and the water vapor in the mixed gas are the same or different, introducing superheated steam to preheat bed materials in the gasification furnace, carrying out oxidation combustion reaction in the gasification furnace, enabling the temperature of the bed layer to be higher than the temperature of the superheated steam, adjusting the proportions of the input oxygen and the steam within a set range, enabling ash slag at the lower part of the gasification furnace not to be melted, and keeping a dry slag state;

performing solid-state slag discharge or liquid-state slag discharge according to needs, wherein during the solid-state slag discharge, the highest temperature layer in the gasification furnace is kept at the middle-lower part of the gasification furnace or the upper part of the fixed material discharge area, and the temperature of the outlet of the gasification furnace is kept at a set temperature; when slag is discharged in a liquid state, a carbon residue cyclone combustion cylinder connected with a gasification furnace is used for combustion, simultaneously, smoke generated by combustion is sent back to the gasification furnace for utilization, solid or liquid produced after combustion enters a slag quencher for cooling and then is discharged, and oxygen and steam are introduced into the carbon residue cyclone combustion cylinder in the combustion process to ensure that the combustion temperature can melt carbon residue;

when gasification stable state treatment is carried out in the gasification furnace, oxygen concentration detection is carried out on the flue gas leaving the carbon residue cyclone combustion cylinder, whether the oxygen concentration is in a set oxygen concentration range is checked, and if the oxygen concentration is not in the set oxygen concentration range, the ash discharging speed is increased or decreased according to the requirement; detecting the temperature of an air outlet of the gasification furnace in real time, if the temperature of the air outlet is continuously increased, increasing the ash discharging speed, and if the temperature of the air outlet is continuously reduced, reducing the ash discharging speed;

when molten slag is formed at the bottom of the gasification furnace and in the ash melting control cylinder, the pressure of the outlet of the pneumatic valve relative to the gasification furnace is adjusted through the flow of make-up gas and the balance pipe valve, the liquid level of molten liquid at the outlet is changed to influence the discharge speed of the liquid slag, so that the liquid level of the molten slag at the bottom of the gasification furnace and in the ash melting control cylinder is kept stable, and the liquid slag in the ash melting control cylinder is continuously sent into a slag quenching device through the pneumatic valve;

when the gasification furnace is stopped, the pressure at the upper part of the quencher is reduced, the molten slag is quickly discharged into the quencher from the bottom of the gasification furnace, the ash melting control cylinder, the pneumatic valve and the like, the normal granular solid enters the ash melting control cylinder and the pneumatic valve, and then the next gasification furnace is waited for cold/hot start.

Technical Field

The invention belongs to the field of gasification furnaces, and particularly relates to a fixed bed gasification furnace and an ash and slag discharging method.

Background

The fixed bed (also called moving bed) gasification furnace is the oldest coal gasification equipment and has the characteristics of mature technology, reliable equipment, flexible production operation, high thermal efficiency in the coal conversion process and the like. Although the modern coal gasification technology has advancement in various aspects such as raw materials, environmental protection and the like, the fixed bed gasification still has proper application prospect, particularly after slag ash discharge is adopted, the processing capacity of the fixed bed gasification under the pressurization condition is obviously improved, and the environmental protection characteristic is improved. The fixed bed gasification furnace has the important characteristics of simple raw material preparation, high methane yield, high value-added tar byproduct and high thermal efficiency compared with other technologies, and particularly has obvious low oxygen consumption, so that the fixed bed gasification furnace has special attraction in the field of coal gasification combined cycle power generation.

The most of fixed bed gasification furnaces have been equipped with a grate which supports the bed material in the furnace and has the function of distributing the gasifying agent, and the grate guides the ash generated in the gasification process to a pressurized ash bin. The large-scale grate has the advantages of complex structure, high investment and maintenance cost and low operation reliability. The slag-tap fixed bed gasification furnace converts ash slag into a molten state at a temperature higher than the ash melting point, liquid flows conveniently, and the gasification furnace has improved generation strength due to the improved gasification reaction temperature, which meets the requirements of modern coal chemical industry. However, the existing slag type fixed bed gasification furnace has the disadvantages of large difficulty in controlling slag, narrow operation window, high requirement and high price of a formed slag pool on nozzle materials, refractory materials and the like of the gasification furnace, and long cleaning and maintenance period and high cost after slag blockage.

Disclosure of Invention

In order to solve the technical problems, the invention provides a fixed bed gasification furnace and an ash and slag discharging method.

In order to solve the technical problems, the invention adopts the following technical scheme:

the utility model provides a fixed bed gasifier, includes the furnace body, the upper end of furnace body is connected with high-pressure feed bin through the passage, and furnace body upper portion is equipped with the gas outlet, is equipped with the temperature measurement pipe in the furnace body upper portion is inside, and the inside thermocouple that is used for measuring temperature that is equipped with the different altitude position of a plurality of temperature measurement pipe, the furnace body lower part are equipped with solid material exhaust area, and the furnace body lower part is equipped with the import of at least two sets of auxiliaries, and the exit end that solid material exhaust area.

The residual carbon treatment mechanism comprises a residual carbon cyclone combustion cylinder and a slag quenching cylinder which are connected, an auxiliary agent introducing port is arranged on the residual carbon cyclone combustion cylinder, and a control valve is arranged at the lower part of the furnace body and connected with the residual carbon cyclone combustion cylinder.

The residual carbon cyclone combustion cylinder and the slag quenching cylinder are both vertically arranged, and the inlet end of the residual carbon cyclone combustion cylinder is connected with the solid material discharge area.

And a discharge controller is arranged in the solid material discharge area.

The residual carbon cyclone combustion cylinder is inclined with a high end and a low end, the slag quenching cylinder is vertically arranged, the control valve is connected to the feeding end of the residual carbon cyclone combustion cylinder, the flue gas return pipe is connected to the side wall of the residual carbon cyclone combustion cylinder, and the inlet end of the residual carbon cyclone combustion cylinder is connected with the solid material discharge area.

The residual carbon cyclone combustion cylinder and the slag quenching cylinder are both vertically arranged, the control valve is connected to the side wall of the residual carbon cyclone combustion cylinder, the solid material discharge area is connected with the side wall of the residual carbon cyclone combustion cylinder, and the flue gas return pipe is connected to the inlet end of the residual carbon cyclone combustion cylinder.

And the outlet end of the fixed material discharge area is connected with a slag tank.

The residual carbon treatment mechanism comprises an ash melting control cylinder and a slag quenching device, the ash melting control cylinder is connected with the outlet end of the solid material discharge area, the bottom of the ash melting control cylinder is connected with a pneumatic valve, the ash melting control cylinder is provided with an auxiliary agent inlet, the slag quenching device is connected with a balance pipe, the balance pipe is connected with the conical bottom area of the gasification furnace, the balance pipe is provided with a release port and a supplementary gas inlet, the pneumatic valve extends obliquely from bottom to top, the higher end of the pneumatic valve is connected with the inlet of the slag quenching port, the lower end of the pneumatic valve is connected with the ash melting control cylinder, and the position of the connection point of the pneumatic valve and the slag quenching device is not less than the height difference of the connection point of the ash melting control cylinder and the pipeline diameter of the pneumatic valve. The outlet pressure of the pneumatic valve is adjusted by controlling the flow of the make-up gas and the valve of the balance pipe to control the discharge speed of the molten slag through the pneumatic valve.

The auxiliary furnace is characterized in that a material baffle plate is arranged in the lower part of the furnace body and is positioned above the connecting position of the residual carbon cyclone combustion cylinder and the furnace body, a space without solids is formed at the bottom of the material baffle plate, so that backflow flue gas can enter and be distributed conveniently, the lower part of the furnace body is in a cone shape, an auxiliary agent introducing port or an auxiliary agent inlet is internally provided with an auxiliary inner air distribution assembly, so that an auxiliary agent can uniformly enter the furnace body, and the auxiliary agent introducing port or the auxiliary agent inlet is used for introducing oxygen.

A method for discharging ash and slag of a fixed bed gasification furnace comprises the following steps:

before starting, filling a part of ash and slag into the bottom of the gasification furnace, filling the ash and slag into the fixed material discharge area, then pre-filling crushed coal on the ash and slag layer to reach the normal material level of the gasification furnace, and filling a high-pressure material bin with the crushed coal through a coal lock for standby;

inputting oxygen and steam from the lower part of the gasification furnace, introducing superheated steam to preheat bed materials in the gasification furnace, carrying out oxidation combustion reaction in the gasification furnace to ensure that the temperature of the bed layer is higher than that of the superheated steam, adjusting the proportion of the input oxygen and the steam within a set range, ensuring that ash and slag at the lower part of the gasified rice are not melted, and keeping the dry slag state;

performing solid-state slag discharge or liquid-state slag discharge according to needs, wherein during the solid-state slag discharge, the highest temperature layer in the gasification furnace is kept at the middle-lower part of the gasification furnace or the upper part of the fixed material discharge area, and the temperature of the outlet of the gasification furnace is kept at a set temperature; when slag is discharged in a liquid state, a carbon residue cyclone combustion cylinder connected with a gasification furnace is used for combustion, simultaneously, flue gas generated by combustion is sent back to the gasification furnace for utilization, solid or liquid produced after combustion enters a slag quencher for cooling and then is discharged, and oxygen and steam are introduced into the carbon residue cyclone combustion cylinder in the combustion process, so that ash with low carbon residue can be melted at the combustion temperature;

when gasification stable state treatment is carried out in the gasification furnace, oxygen concentration detection is carried out on the flue gas leaving the carbon residue cyclone combustion cylinder, whether the oxygen concentration is in a set oxygen concentration range is checked, and if the oxygen concentration is not in the set oxygen concentration range, the ash discharging speed is increased or decreased according to the requirement; and detecting the temperature of the gas outlet of the gasification furnace in real time, if the temperature of the gas outlet is continuously increased, increasing the ash discharging speed, and if the temperature of the gas outlet is continuously reduced, reducing the ash discharging speed.

The invention obviously simplifies the air distribution structure and the ash discharge structure of the reaction gas of the gasification furnace, can directly carry out dry ash discharge control, separates the processes of carbon residue combustion and ash slag melting from the gasification furnace body when the operation range of slag needs to be entered, adopts small combustion equipment to complete the ash slag melting operation, accurately controls the ash discharge and the ash discharge of the gasification furnace, simplifies the operations of starting, stopping, heat preparation and the like of the gasification furnace, is obviously beneficial to improving the reliability and the availability of the fixed bed gasification furnace, and realizes the discharge of solid slag and liquid slag.

Drawings

FIG. 1 is a schematic view of an embodiment of the present invention;

FIG. 2 is a schematic top view of a furnace body according to a first embodiment of the present invention;

FIG. 3 is a schematic view of a second embodiment of the present invention;

FIGS. 4 and 5 are schematic views of a partially cut-away structure of the furnace body with different viewing angles in the second embodiment;

FIG. 6 is a schematic structural diagram of a third embodiment of the present invention;

FIG. 7 is a schematic structural diagram of a fourth embodiment of the present invention;

FIGS. 8 and 9 are schematic views of partial structures of furnace bodies at different viewing angles in the fourth embodiment;

fig. 10 is a schematic structural diagram of a fifth embodiment of the present invention.

Detailed Description

For further understanding of the features and technical means of the present invention, as well as the specific objects and functions attained by the present invention, the present invention will be described in further detail with reference to the accompanying drawings and detailed description.

As shown in attached figures 1 and 2, the invention discloses a fixed bed gasification furnace, which comprises a furnace body 5, wherein the upper end of the furnace body 5 is connected with a high-pressure bin 2 through a material guide pipe 3, the upper part of the furnace body 5 is provided with a gas outlet 8, the gas outlet is used for outputting generated coal gas outwards, a temperature measuring pipe 4 is arranged in the upper part of the furnace body 5, a plurality of thermocouples with different height positions are arranged in the temperature measuring pipe for measuring temperature, the lower part of the furnace body 5 is provided with a solid material discharging area 7, the lower part of the furnace body 5 is provided with at least two groups of auxiliary agent inlets, and the outlet end of the solid material. The gas outlet is used for discharging coal gas generated by the reaction, and ash and slag are discharged from the fixed material discharge area, and are discharged to a designated position after reaching the carbon residue treatment mechanism for treatment. The high-pressure bin is connected with a pressurized coal lock, and the upper position and the lower position of the pressurized coal lock are provided with a pressurized valve which can pressurize materials. The auxiliary agent inlet is mainly used for inputting oxygen, air and water vapor and used for auxiliary heating or used as reaction gas. The auxiliary agent inlets can be a plurality of spraying groups, so that the gas is conveniently conveyed. The direction of the arrow in FIG. 1 indicates the reaction gas input position, i.e., the auxiliary agent input position.

The guide pipes and the temperature measuring pipes can be arranged in a plurality of ways, in the embodiment, three guide pipes are arranged, the three guide pipes are divided into three ways to be connected with the top of the furnace body, screened normal-pressure crushed coal with the general particle diameter of 6-50 mm is added into the pressurizing coal lock, the pressurizing is carried out by the pressurizing coal lock, the pressure can be from low pressure to high pressure of 10MPa, the crushed coal after pressurizing is sent to a pressure bin positioned at the top of the furnace body, the guide pipes at the bottom of the pressure bin are connected with the top of the furnace body, and pressure lump coal moves to a stable material layer height on the upper part of the furnace body through.

Once the material level of the high-pressure bin reaches the low limit, the pressure coal lock is responsible for conveying pressure lump coal to the high-pressure bin and keeping the high-pressure bin always filled with the material. Therefore, the material is always kept in the material guide pipe, and as long as the material level in the gasification furnace moves downwards, the coal in the material guide pipe moves downwards to supplement the coal material at any time, so that the material level on the upper surface of the gasification furnace is kept constant, and the sufficiency of the material is ensured. Because the feeding into the gasification furnace through the material guide pipe does not have the process of free falling, the fine coal powder in the falling process is prevented from being carried by the ascending gas flow and being taken out of the gasification furnace, and the dust content of the outlet gas is low.

Through many temperature tubes, the not co-altitude temperature of measurable quantity gasifier bed of material. The temperature uniformity conditions of different positions of the section of the gasification furnace can be tracked at any time by arranging the plurality of temperature measuring pipes. The bottom of the furnace body is provided with temperature measuring elements with different insertion depths along the circumference at different heights, so that the temperature of different positions can be measured, and more accurate control can be performed.

In addition, the structure of the furnace body is divided into a furnace body upper part, a furnace body middle part and a furnace body lower part, the furnace body middle part has a structure from small to large, the furnace body lower part is in a cone shape, the upper part is a coal material inlet and coal gas outlet area, the middle part is a main reaction area, and the lower part is a carbon residue combustion area and is used for discharging ash and slag.

As shown in fig. 6, the middle part of the furnace body is of a structure from small to large, the expansion of the sectional area is beneficial to the outward stretching of the accumulated coal, and the cracking among coal particles can be assisted, the aggregation can be reduced and the air permeability can be improved when the coal with weak caking property is used; on the other hand, the friction force received by the inner side surface of the gasification furnace from solids is reduced by enlarging the section, which is beneficial to protecting the inner surface structure of the gasification furnace.

In the gasification furnace, lump coal added to the upper part of the gasification furnace is in countercurrent contact with hot gas from the bottom, the coal material is dried and dehydrated, distilled and dehydrated to volatilize, and then semicoke reacts with water vapor and carbon dioxide in the gas to carry out gasification reaction to generate CO and H₂The residual carbon left after gasification enters the bottom of the gasification furnace. At the bottom of the gasification furnace, pure oxygen or air and part of water vapor are introduced into the gasification furnace, the oxygen burns the carbon residue, the carbon dioxide and the water vapor are heated by combustion heat and flow upwards along with hot air flow, and the contained heat supplies energy required by gasification reaction, dry distillation and drying. After the carbon residue is almost burned out, the remaining substances are ash residues converted from inorganic substances contained in the raw coal.

The bottom of the furnace body is designed to be a cone with a small angle, and an opening at the bottom of the cone is a solid material discharge area for discharging ash slag. The different heights of the furnace body cone are provided with a plurality of groups of inlets for gasification reaction gas (oxygen or air, water vapor, carbon dioxide and the like) along the periphery, the gas at different heights can adopt gasification gas components with different proportions, such as different proportions of water vapor and oxygen, and the flow of the reaction gas entering at different heights is different according to the sectional area of the gasifier to be covered. After oxygen in the gasified gas enters the cone, the oxygen and carbon residue in the solid material are subjected to combustion reaction, the carbon residue is combusted, and a large amount of heat is released. The combustion heat release heats the water vapor and the carbon dioxide generated by the combustion to raise the temperature, the high-temperature gas continuously rises, and the high-temperature gas and the residual semicoke after the dry distillation and the devolatilization are subjected to gasification reaction. The reaction gas with lower temperature is contacted with the produced ash slag in a counter-current way after the combustion is finished, the ash slag is cooled, and the gas is continuously subjected to combustion reaction with carbon residue after the temperature is raised. The proportion of the water vapor and the oxygen in the gasification reaction gas can be adjusted, and the gasification reaction gas can be properly adjusted according to different conditions, so that the discharge of solid materials or liquid materials is realized.

For setting the taper angle at the lower part of the furnace body, the solid movement of the straight cylinder section of the gasification furnace is ensured to always keep uniform flow. The angle of taper is in the range 10-60 deg., preferably between 20-40 deg..

Different schemes are provided for the connecting structure of the fixed body discharging area at the lower part of the furnace body.

In the first embodiment, as shown in fig. 1, a transverse discharging controller 5 is arranged in a fixed material discharging area 7, and the fixed material discharging area 7 is connected with an ash tank 6, wherein the spiral feeding structure is adopted. And moving the cooled solid particle ash to an outlet of a solid material discharge area at the bottom of the cone of the gasification furnace. By arranging the discharge controller in the solid material discharge area, the discharge controller can be a plurality of mechanisms including a transverse screw, a vertical screw, a small-sized grate and the like, and the spiral feeding structure discharges ash from the solid material discharge area to the ash tank and then from the ash tank to a specified position. The spiral feeding structure comprises a cooling heat exchange surface to further cool ash, and the ash discharging speed can be controlled by the change of the rotating speed of the spiral. Therefore, the problem that the conventional gasification furnace needs a furnace grate with the same diameter as the gasification furnace is avoided, and the furnace grate is complex in structure, high in cost and high in operation and maintenance requirements. Thereby reducing equipment costs.

In the second embodiment, as shown in fig. 3 to 5, the carbon residue treatment mechanism includes a carbon residue cyclone combustion cylinder 11 and a slag quenching cylinder 12 which are connected, the carbon residue cyclone combustion cylinder 11 is inclined with a higher end and a lower end, the slag quenching cylinder 12 is vertically arranged, a control valve 10 is connected to a feed end of the carbon residue cyclone combustion cylinder 11, a flue gas return pipe 9 is connected to a side wall of the carbon residue cyclone combustion cylinder 11, and an inlet end of the carbon residue cyclone combustion cylinder 11 is connected to the solid material discharge area 7. The discharge controller is vertically disposed within the solids discharge zone. The gas can be extracted from the flue gas return pipe for oxygen concentration analysis. The direction of arrows in fig. 3 indicates the reaction gases (oxygen and water vapor) supplied at various positions.

After the coal material is gasified and reacted in the furnace body, the solid particle size is greatly reduced along with the completion of the semicoke gasification reaction, and the carbon content in the solid containing residual carbon and mineral substances is 50-70%. At the very bottom of the cone zone into the bottom of the gasifier, the solids remain in a solid particulate state. When a lower ratio of water vapor to oxygen is fed into the furnace body, the gasification of the semicoke is mainly completed in the upward direction of the lower conical bottom area in the furnace body, the residual carbon combustion is not performed here, but the inorganic solid containing the residual carbon is discharged from the solid material discharge area.

Oxygen and water vapor are introduced through the control valve, solid materials in the solid material discharge area are fluidized, the materials are pushed to the residual cyclone carbon combustion cylinder, meanwhile, the solid materials in the conical section at the lower part of the furnace body are continuously supplemented to the solid material discharge area, the speed of pushing the solid materials can be directly determined by the size of gas flow led to the control valve, and therefore the speed control of solid material discharge at the conical bottom of the gasification furnace can be achieved. Oxygen and water vapor are also introduced into the residual carbon cyclone combustion cylinder during combustion.

The solid particles leaving the control valve and the solid material discharged from the discharge controller are combined together and enter the feeding end of the carbon residue cyclone combustion cylinder, and the reaction gas (oxygen and water vapor) rapidly enters the carbon residue cyclone combustion cylinder from the feeding end along the tangential direction. Oxygen and water vapor are introduced into the carbon residue cyclone combustion cylinder, and the solid materials possibly settled to the bottom of the carbon residue cyclone combustion cylinder are rotated again so as to be convenient for contacting with the oxygen and ensure the complete burning of the carbon residue.

In the carbon residue cyclone combustion cylinder, carbon residue in the solid is rapidly combusted by oxygen until the carbon residue is burnt out. The temperature is raised by the heat released by combustion and exceeds the ash melting point temperature of the mineral substances, and then the solid ash is converted into molten slag. The cyclone combustion cylinder is obliquely arranged, so that molten slag can flow to the other end, flows out from the end, falls into the slag quencher and is chilled by water to be solidified. The solidified ash is discharged out of the pressure system through a slag lock.

In addition, a material baffle plate 14 is arranged in the lower part of the furnace body 5, the material baffle plate 14 is positioned above the connecting position of the residual carbon cyclone combustion cylinder 11 and the furnace body 5, the lower part of the furnace body is in a cone shape, an auxiliary inner air distribution assembly is arranged in an auxiliary agent introducing port or an auxiliary agent inlet, so that the auxiliary agent uniformly enters the furnace body, and the auxiliary agent introducing port or the auxiliary agent inlet is used for introducing oxygen and water vapor. Above the residual carbon combustion flue gas entering the airflow direction of the cone bottom area, the baffle plate arranged in the cone bottom area is slightly wider than the airflow overall dimension, and the baffle plate provides a flowing space for the gas entering the deep part in the cone bottom area and is beneficial to uniform distribution.

The second embodiment can achieve the purpose of discharging solid materials according to requirements.

In the third embodiment, as shown in fig. 6, the carbon residue cyclone combustion cylinder 11 and the slag quenching cylinder 12 are both vertically arranged, the control valve 10 is connected to the side wall of the carbon residue cyclone combustion cylinder 11, the solid material discharge area 7 is connected to the side wall of the carbon residue cyclone combustion cylinder 11, and the flue gas return pipe 9 is connected to the inlet end of the carbon residue cyclone combustion cylinder 11, and belongs to a vertical furnace structure. The control valve and the residual carbon cyclone combustion cylinder are connected in a tangential mode and are cut into the circumferential direction of the side wall. The arrow direction in fig. 6 indicates the reaction gas (oxygen and water vapor) supplied at each position.

The gas flow introduced into the control valve 10 pushes the solid material to the carbon residue cyclone combustion cylinder, more oxygen is added into the solid flow from the control valve, and the oxygen and the solid flow tangentially and rapidly enter the carbon residue cyclone combustion cylinder. The solid carbon residue from the solid material discharge area is at a high temperature, such as 1000 ℃ or above, and once oxygen contacts the carbon residue, the carbon residue is combusted, and the combustion releases heat to raise the temperature, so that the solid after the carbon residue is combusted is possibly higher than the melting temperature to form slag. With the rotation, the slag flows downwards along the wall of the cylinder and finally flows into a slag quenching cylinder at the bottom for cooling. And an additional oxygen inlet is also arranged below the solid material inlet to continuously provide enough oxygen for the combustion of the residual carbon, and the additional oxygen also enters the combustion cylinder in a tangential manner to increase the time for the solid to rotate along the cylinder wall, so that the residual carbon is completely burnt.

In the third embodiment, the slag in a molten state is formed by high-temperature combustion, and the slag is discharged as a liquid material.

In the fourth embodiment, as shown in fig. 7 to 9, the carbon residue cyclone combustion cylinder and the slag quenching cylinder are both vertically arranged, and the inlet end of the carbon residue cyclone combustion cylinder is connected with the solid material discharge area. This fourth embodiment is opposite to the third embodiment, and no flue gas return pipe is separately provided. The arrow direction in fig. 7 indicates the reaction gas (oxygen and water vapor) supplied at each position.

Because carbon residue whirlwind combustion section of thick bamboo 11 directly sets up in solid material exhaust area 7 below, control valve 10 one end and furnace body 5 sub-unit connection, the control valve 10 other end is connected with carbon residue whirlwind combustion section of thick bamboo 11, this connection be with the circumference tangential direction of combustion chamber barrel. Oxygen enters the carbon residue cyclone combustion cylinder from the tangential direction. And a part of solid materials are directly discharged to the residual carbon cyclone combustion cylinder from a solid material discharge area at the bottom of the furnace body, and the other part of solid materials are controlled by the input reaction gas through the control valve, the residual carbon-containing solid is fed into the residual carbon cyclone combustion cylinder from the tangential direction together with the other input group of reaction gas, oxygen is contacted with the residual carbon to burn the residual carbon, the molten slag flows down to the slag quenching cylinder at the bottommost along the wall surface of the combustion chamber, and high-temperature flue gas generated by combustion rises to enter the conical bottom of the furnace body. Under this scheme, the gas velocity of flow who leaves the combustion chamber sets up to enough high, avoids gasifier awl end solid material directly to drop to carbon residue whirlwind burning section of thick bamboo. An auxiliary air distribution assembly 15 can be arranged in the furnace body, so that the air discharged into the furnace body can be more uniform.

Fifth embodiment, as shown in fig. 10, the carbon residue treatment mechanism includes an ash melting control cylinder 16 and a slag quenching device 17, the ash melting control cylinder 16 is connected to the outlet end of the solid material discharge area 7, the bottom of the ash melting control cylinder 16 is connected to an air valve 18, the ash melting control cylinder 16 is provided with an auxiliary agent inlet, the slag quenching device 17 is connected to a balance pipe 19, the balance pipe 19 is provided with a discharge port 20, the air valve extends obliquely from bottom to top, and the high end of the air valve is connected to the inlet of the slag quenching port, the low end of the air valve is connected to the ash melting control cylinder, the difference between the heights of the high end and the low end is greater than one pipe diameter, and the balance pipe is provided with a valve. The upper part of the quencher is provided with a supplementary gas pipe 21 which is controlled by supplementary gas flow and a balance pipe valve, the relative pressure between the outlet of the pneumatic valve and the gasification furnace is adjusted by utilizing the gas seal function of the ash separation melting control cylinder and the quencher when the pneumatic valve is filled with liquid, mainly the pressure at the upper part of the slag quencher influences the liquid level at the outlet end of the pneumatic valve, and the discharge speed of the molten slag through the pneumatic valve is controlled. The dispersion port is mainly used for starting and stopping the gasification furnace, when the gasification furnace is stopped, the balance pipe valve is closed, the dispersion port is quickly opened, the liquid molten slag in the cone bottom area, the ash melting control cylinder, the pneumatic valve and the like can be quickly discharged into the quenching device by the low pressure of the outlet of the pneumatic valve, so that the ash melting control cylinder and the pneumatic valve are filled with normal granular solid materials which are not melted, and the gasification furnace can be conveniently started again in a cold/hot mode next time. The arrow direction in fig. 10 indicates the reaction gas (oxygen and water vapor) supplied at each position. The position of the connecting point with the slag quenching opening is higher than the position of the connecting point with the ash fusion control cylinder.

Oxygen is mainly introduced into the ash melting control cylinder in the reaction gas, the oxygen burns residual carbon contained in solids from a conical bottom area of the furnace body, and the solid ash is changed into a molten state by combustion heat release. Reaction gas and auxiliary fuel gas are introduced into the pneumatic valve and are mainly used for heating when the system is started, and in the normal operation process, the temperature is continuously increased through the combustion of oxygen and fuel at the position to ensure that molten slag has good fluidity and flows to a slag quenching device through a flat pipe section of the L valve. When the ash is in a solid state, the ash has almost no fluidity, under the condition that no airflow flows to the outlet direction of the pneumatic valve, the solid is not easy to move to the outlet direction of the pneumatic valve from the vertical direction, and once the ash becomes flowable molten slag, the liquid can flow to the slag quencher through the flat pipe section of the pneumatic valve. The dry ash at the bottom of the furnace body moves downwards to continuously participate in carbon residue combustion along with the dry ash in the ash melting control cylinder (also comprising the conical bottom of the furnace body) being combusted, heated and melted and flowing out of the bottom of the ash melting control cylinder, and finally the purpose of slag discharge of the gasification furnace is achieved. The pneumatic valve is arranged in an inclined and tilted shape and mainly plays a role of air sealing, namely when the flat pipe section of the L-shaped valve is filled with liquid molten slag, air at the upper part of the quencher cannot flow to the ash melting control cylinder from the horizontal pipe section, and the possibility that solids flow out along with liquid is reduced as much as possible. The balance pipe of the gas can remove redundant gas from the upper part of the slag quencher, a supplementary gas connecting line is also arranged on the upper part of the slag quencher, when the pressure of the quencher is required to be increased, nitrogen and other gases are introduced, and the discharge speed of the slag is controlled to be matched with the reaction production speed of the gasification furnace through the control of a valve on the balance pipe, the flow of the supplementary gas and the control of a valve of a release pipeline. Besides the above described profile L-valve, the configuration of the pneumatic valve can also be U-shaped, etc. Scheme example five is also applicable to other types of gasifier hearth structures, such as conventional flat-bottomed or round-bottomed type gasifiers.

In the above embodiments, a plurality of oxygen and steam can be selectively introduced, and a proper proportion and an appropriate number of input paths are selected according to actual requirements, so as to meet normal gasification reaction and slag discharge requirements. On the pipe section before the outlet of the shaped L-valve, auxiliary combustion may be provided as required to maintain the fluidity of the slag, not shown in the figure.

When the gasification furnace is used for gasification treatment, oxygen and water vapor are mainly introduced into the lower part of the furnace body and enter the conical area at the bottom of the furnace body, and partial reaction gas can enter the furnace body by means of the auxiliary air distribution assembly arranged in the furnace body according to use requirements, so that the distribution of the reaction gas is more uniform.

The furnace body does not directly generate combustion reaction and basically does not contact extreme high temperature, so the furnace body can adopt common refractory materials, and the cast-in-place refractory material can also be suitable. Two or three layers of cast refractory may be used, with the innermost layer being a refractory material with good wear resistance, such as a high alumina refractory material. In the cone bottom area of the gasification furnace, a solidified ash layer is formed on the surface of the refractory material by partial slag due to the heat dissipation of the shell, so that the refractory material is protected. At the position related to the molten slag, the heat loss needs to be reduced as much as possible through the selection and thickness design of refractory materials, the blockage caused by solidification and deposition of a large amount of molten slag after the pipe wall and the wall are cooled is avoided, and necessary external heating measures can be set according to the needs.

The invention also provides an ash discharge and slag discharge method of the fixed bed gasification furnace, which comprises the following steps:

before starting, a part of ash is filled into the bottom of the gasification furnace, at the moment, the fixed material discharge area is also filled with the ash, then, crushed coal is pre-filled on the ash layer to reach the normal material level of the gasification furnace, and the high-pressure material bin is filled with the material through a coal lock for standby.

When the gasifier is ready to start, reaction gas (oxygen and water vapor) is input from the conical bottom of the gasifier body, superheated steam is introduced to preheat bed materials, then pure oxygen is gradually added, and the temperature of each layer at different height positions in the gasifier can be detected through temperature measuring tubes arranged in the gasifier. After the oxidative combustion reaction has started significantly, the bed temperature will be higher than the superheated steam temperature. The proportion of the input water vapor and the input oxygen is adjusted within the range of 4-8, and the principle is to ensure that ash slag generated in the bottom area of the gasification furnace cone is not melted and the dry slag state is maintained. Until the temperature gradient of each layer of the gasification furnace reaches the normal working condition. The ratio of the water vapor to the oxygen of each reaction gas series can be independently set and adjusted according to requirements.

As for the slag discharge mode, there are solid slag discharge and liquid slag discharge schemes.

For the solid slag discharging scheme, as shown in fig. 1, after the temperature gradient of the gasifier reaches the temperature, the bottom spiral type discharging controller is started to discharge ash, the highest temperature layer in the bed is moved downwards and controlled at the lower part of the gasifier or at the upper part of the conical bottom area, and the temperature of the coal gas outlet at the upper part of the gasifier also reaches the set range. Some temperature measuring points can be arranged at the conical bottom of the furnace body, the temperature of the residual carbon combustion in the conical bottom area is judged by using the temperature measuring points, and the mixing ratio of the whole water vapor and the oxygen is adjusted by the characteristic of discharging dry ash, so that the efficiency of the gasification process is optimal.

For the slagging solution, as shown in fig. 3, a gas burner (not shown) on the carbon residue cyclone combustion cylinder is started, and the refractory material of the combustion chamber and the refractory material of the flue gas outlet pipe are preheated by the heat generated by burning the gas. And then, discharging materials to the residual carbon cyclone combustion cylinder from a solid material discharge area at the bottom of the furnace body through a control valve, introducing oxygen to the residual carbon cyclone combustion cylinder, introducing solid or liquid produced after combustion into a slag quenching cylinder, and introducing reaction gas into the conical bottom of the gasification furnace from the top. As the temperature of the solid from the conical bottom of the gasification furnace is increased and enough residual carbon is contained, the temperature of the combustion chamber can reach a temperature higher than the ash melting point, the solid is changed into slag after combustion, and finally the slag quenching cylinder is cooled.

At different positions of the gasification furnace, a plurality of paths of reaction gases are respectively input, the reaction gases in different paths are all composed of water vapor and oxygen or air, and the water vapor and the oxygen and the proportion can be correspondingly set according to the coal type, the mineral content, the ash melting point, the production conformity and the operation pressure.

During steady-state operation, the high-pressure bin always keeps materials, the material level at the upper part in the gasification furnace is stable under the action of the material guide pipe, and solid carbon residue and mineral substances enter the conical bottom of the gasification furnace along with the progress of drying, dry distillation and gasification in the gasification process. The discharge controller continuously discharges the solid materials to the residual carbon cyclone combustion cylinder, the residual carbon is combusted by pure oxygen, and the high-temperature flue gas returns to the cone bottom area to supply heat to the gasification reaction. Most of oxygen enters the carbon residue cyclone combustion cylinder for carbon residue combustion, and a small part of oxygen directly enters the gasification furnace through the conical bottom of the gasification furnace. The ash discharge speed corresponds to the gasification reaction capacity, the residual carbon content in the discharged ash is almost completely burnt by the introduced oxygen, and the flue gas leaving the residual carbon cyclone combustion cylinder contains low-concentration oxygen, such as 0.5-2%, and generally less than 1%. The oxygen concentration was obtained by on-line gas sampling analysis. The change trend of the temperature of the gas outlet is an important index for reflecting whether the operation of the gasification furnace is stable, and when the gas at the gas outlet continuously rises, the coal layer in the furnace moves upwards, and the ash discharge speed needs to be increased. If the ash discharging speed is too high, the oxygen flow during the burning of the residual carbon is not enough to consume the whole residual carbon, no residual oxygen exists in the flue gas at the outlet of the residual carbon cyclone combustion cylinder, and the carbon ash in the discharged ash is increased. Therefore, the method can be indirectly or directly used for controlling the ash discharge speed of the gasification furnace by monitoring parameters such as the gas outlet temperature of the gasification furnace, the temperature gradient of each layer in the bed, the oxygen concentration in the residual carbon combustion flue gas, carbon content in the discharged slag and the like. For the operation of the fixed bed gasification furnace, the operation of the gasification furnace is more stable through accurate ash discharge and slag discharge.

A plurality of groups of temperature measurement can be arranged in the furnace body, and the method is mainly used for judging whether the gasifier is uniformly distributed on the whole section.

When the gasification furnace is ready to stop, the proportion of the water vapor and the oxygen in the reaction gas can be adjusted firstly, the mixing proportion is improved, then the ash discharge from the cone bottom area of the gasification furnace is stopped, the oxygen supply to the carbon residue cyclone combustion cylinder is stopped, and the gasification furnace can enter a hot standby state after the water vapor is blown and swept for a period of time. When emergency stop is needed, the L gas and all oxygen gas flow can be directly stopped, steam purging is carried out briefly, and the gasification furnace is provided with safe hot equipment.

When the gasification furnace is restarted from a hot standby state, reaction gas is input at different positions, and the ratio of water vapor to oxygen is properly increased in each reaction gas series; starting the control valve to discharge materials and oxygen combustion of the residual carbon cyclone combustion cylinder, enabling the gasification furnace to basically enter an operation state, and then adjusting the proportion of water vapor and oxygen in each reaction gas to a normal state to enable the gasification furnace to stably operate.

The operation of the molten slag can be suitable for the operation of coal types with wide coal ash melting points, but the operation of the coal types with medium and low ash melting points (such as FT (FT) at 1100-1350 ℃) is more preferable, at this time, if the operation temperature of the gasification furnace is too low, the processing capacity of the gasification furnace cannot be improved, and the operation of the molten slag can allow the gasification furnace to be operated at higher temperature, such as 1500-1800 ℃, and the reaction at high temperature can obviously improve the gasification effect.

In actual operation, for the gasification of coal with high ash fusion point, the gasification furnace is normally operated, the carbon residue cyclone combustion cylinder also normally burns out carbon residue, but ash particles can still keep a solid state and are sent to the quencher for cooling. The same gasification and ash removal effects can be achieved.

For the operation of coal with extremely high ash melting point, the ratio of water vapor to oxygen in the reaction gas is flexibly adjusted, so that the residual carbon is finished at the conical bottom of the gasification furnace, and the gasification furnace operation can be carried out according to the scheme shown in fig. 1. 2 paths of reaction gas are input into the conical bottom of the gas furnace, and then one path of reaction gas is input into the solid material discharge area.

Because the coal ash melting operation is carried out outside the gasification furnace, the reaction gas used for residual carbon combustion can be mainly oxygen alone, and the 2-path reaction gas at the conical bottom of the gasification furnace can be independently combusted with the residual carbon. The water vapor proportion in the reaction gas is properly increased, the water gas shift reaction in the gasification furnace can be promoted, more hydrogen components can be obtained, the load of downstream catalytic change can be greatly reduced, the generation amount of the methane component is increased, the oxygen consumption is further reduced, and the overall energy conversion efficiency is improved.

In addition, the gaseous reactant gases enter the gasifier through a plurality of series of nozzle sets, each series including a plurality of sets of nozzles. The ratio of water vapor to oxygen in the reaction gas of each series can be set independently, and the flow distribution between the series can be changed differently according to the operation state of the gasification furnace. After each series of reaction gas enters the gasification furnace, the gas is naturally redistributed in the gasification furnace, and the bed layer in the middle of the gasification furnace adopts the height as high as possible, which is beneficial to the redistribution of the gas on the whole section. An auxiliary air distribution assembly is arranged in the cone bottom area of the gasification furnace according to requirements, so that the redistribution of the gas is facilitated, as shown in fig. 8. In operation, the gasification reaction is carried out at the highest temperature in the middle of the gasification furnace including the conical bottom by adopting a proper ratio of water vapor to oxygen, and simultaneously, ash is not melted, so that the solid is favorably kept in a larger and more uniform granularity, and the reaction gas is favorably and maximally and uniformly distributed in the gasification furnace. After the main semicoke in the coal is gasified, the ratio of the residual carbon to the mineral substances can be in the range of 2: 1 to 1: 1, where there is still carbon residue separation between the ash particles, and thus the opportunity for agglomeration between ash particles is limited despite the moderately high temperatures. The original composition of the coal mineral is an internal factor affecting the morphology of the solids reaching the cone bottom region of the gasifier, and the steam/oxygen ratio is an external factor. The proper configuration of the reaction gas in each series and the proper ash discharge speed control are adopted, so that the carbon residue part needing to be burnt is generated at the conical bottom of the furnace body as little as possible, but is burnt out outside the conical bottom of the gasification furnace as much as possible, and the improvement of the solid granulation in the conical bottom area is facilitated, thereby facilitating the uniform distribution of the reaction gas.

The fixed bed gasification furnace can be suitable for generating synthesis gas with medium and low heat value from low-pressure gasification to producing synthesis gas required by pressurized chemical industry or power generation under high pressure, the operation pressure of about 4.0MPa can be applied to the requirements of coal gasification combined cycle power generation and general chemical industry synthesis such as synthetic ammonia and the like, the synthesis gas pressure obtained by the operation pressure of about 6.5 just meets the requirement of downstream methanol synthesis, and the requirement of recompression of the synthesis gas is avoided. The higher pressure (such as 10MPa) is adopted to be beneficial to improving the concentration of methane in the synthesis gas, the process is very beneficial to carrying out the production process of the substitute natural gas, and the thermal efficiency of the whole production process is more optimized.

Inputting oxygen and steam from the lower part of the gasification furnace, introducing superheated steam to preheat bed materials in the gasification furnace, carrying out oxidation combustion reaction in the gasification furnace to ensure that the temperature of the bed layer is higher than that of the superheated steam, adjusting the proportion of the input oxygen and the steam within a set range, ensuring that ash and slag at the lower part of the gasified rice are not melted, and keeping the dry slag state;

performing solid-state slag discharge or liquid-state slag discharge according to needs, wherein during the solid-state slag discharge, the highest temperature layer in the gasification furnace is kept at the middle-lower part of the gasification furnace or the upper part of the fixed material discharge area, and the temperature of the outlet of the gasification furnace is kept at a set temperature; when slag is discharged in a liquid state, a carbon residue cyclone combustion cylinder connected with a gasification furnace is used for combustion, simultaneously, smoke generated by combustion is sent back to the gasification furnace for utilization, solid or liquid produced after combustion enters a slag quencher for cooling and then is discharged, and oxygen and steam are introduced into the carbon residue cyclone combustion cylinder in the combustion process to ensure that the combustion temperature can melt carbon residue;

when gasification stable state treatment is carried out in the gasification furnace, oxygen concentration detection is carried out on the flue gas leaving the carbon residue cyclone combustion cylinder, whether the oxygen concentration is in a set oxygen concentration range is checked, and if the oxygen concentration is not in the set oxygen concentration range, the ash discharging speed is increased or decreased according to the requirement; and detecting the temperature of the gas outlet of the gasification furnace in real time, if the temperature of the gas outlet is continuously increased, increasing the ash discharging speed, and if the temperature of the gas outlet is continuously reduced, reducing the ash discharging speed.

Through the structural design, the invention has the following characteristics:

1. the high-pressure storage bin and the material guide pipe are arranged, and direct feeding of the material guide pipe is utilized, so that the material level at the upper part of the gasification furnace is ensured to be stable, and coal dust falling is avoided being carried before coal gas leaves the gasification furnace.

2. The temperature measurement pipes which are stretched into the gasifier are arranged, so that real-time temperature measurement at different positions is realized, the temperature at each position of the section of the gasifier and at each position of the height of a bed layer can be tracked and monitored, and the actual working condition in the gasifier can be accurately mastered.

3. The middle part of the gasification furnace adopts a gradually enlarged size, which is beneficial to gas air distribution and protects the inner surface of the gasification furnace.

4. The bottom of the gasification furnace is arranged to be conical, so that residual carbon and solid ash for completing main gasification reaction are discharged from an outlet of a solid material discharge area at the conical bottom of the furnace body, large-scale rotating equipment is avoided, and the cost is saved.

5. The gasification reaction gas is divided into multiple paths to be fed into the gasification furnace according to the requirement, and the reaction of different paths

The ratio of gas, oxygen and water vapor can be independently adjusted to meet different reaction requirements.

6. The solid ash containing the residual carbon enters the residual carbon cyclone combustion cylinder through the control valve or the spiral control, and the oxygen burns the residual carbon.

a. The molten slag formed at the lower part of the cone bottom area of the gasification furnace is continuously fed into a molten slag quenching cylinder through a corresponding control valve for cooling.

7. The slag formed by burning the residual carbon is cooled by water in the quencher instead of being directly discharged.

8. High-temperature flue gas generated by burning the residual carbon is returned to the conical bottom of the gasification furnace, and heat is required by semicoke gasification reaction, so that cyclic utilization is formed.

9. The gasification furnace is convenient to start, stop, hot standby and hot start, and no large solidified slag is left in the gasification furnace every time the gasification furnace is stopped

10. The ash discharge at the conical bottom of the gasification furnace can be flexibly arranged and operated according to different coal types and different process requirements.

a. And (3) ash is discharged by a dry method, the combustion of the residual carbon in the cone bottom area is finished, the combustion temperature is low, no slag is generated, and the ash discharge speed of the dry ash is controlled by an L valve, as shown in figure 1.

b. And discharging ash from the molten slag, namely finishing the combustion of residual carbon at high temperature in a molten slag control area at the bottommost part or the lower part of the conical bottom of the gasification furnace to directly generate the molten slag, and continuously discharging the molten slag to a quencher for cooling through a special-shaped L valve, wherein the step is shown in figure 10.

c. The incompletely burnt carbon residue is discharged from the cone bottom area of the gasification furnace in a solid state, the ash discharge speed is controlled by a control valve, the carbon residue is sent to a combustion chamber for high-temperature combustion, and the molten slag enters a molten slag quenching cylinder for cooling, which is shown in figure 3.

Through the setting, the treatment of different modes can be realized, the processes of carbon residue combustion and ash slag melting are separated from the gasification furnace body, the ash slag melting operation is completed by adopting small combustion equipment, the ash discharge and the slag discharge of the gasification furnace are accurately controlled, the operation of start-stop hot standby of the gasification furnace is simpler and easier, the generated slag is easily discharged from the conical bottom area of the gasification furnace, the molten slag control area, the special-shaped L valve and other parts when the gasification furnace is stopped, the cold/hot start is carried out again under the condition that no large solidified slag exists next time, and the reliability and the availability of the fixed bed gasification furnace are obviously improved.

Although the present invention has been described in detail with reference to the embodiments, it will be apparent to those skilled in the art that modifications, equivalents, improvements, and the like can be made in the technical solutions of the foregoing embodiments or in some of the technical features of the foregoing embodiments, but those modifications, equivalents, improvements, and the like are all within the spirit and principle of the present invention.