CN214619576U - Organic solid waste gasification incineration system - Google Patents

Abstract

The utility model discloses an organic solid useless gasification system of burning, the system includes fixed bed gasifier, second combustion chamber, exhaust-heat boiler and gas heater, and the fixed bed gasifier includes feed arrangement, reaction zone furnace body, top of a furnace gasification agent air inlet, middle section gasification agent air inlet, stove bottom gasification agent air inlet, coal gas outlet and arranges the sediment device. The utility model has the main advantages that the gasification furnace main body equipment has simple structure and low requirements on the types and the granularity of raw materials; the middle part of the material layer is extended to discharge gas, so that fly ash and tar in the fuel gas are adsorbed by the material layer in the conveying process, and the content of the fly ash in the fuel gas is low; the preheated air and the steam generated by the waste heat boiler and the gas preheater are used as gasifying agents to return to the gasification furnace, so that the gasification efficiency and the comprehensive heat utilization efficiency are improved.

Description

Organic solid waste gasification incineration system

Technical Field

The utility model relates to a solid useless processing deals with and the resourceful field, particularly, the utility model relates to an organic solid gasification system of burning that gives up.

Background

The organic solid waste refers to solid organic articles and substances which are produced in production, life, consumption and other activities and lose original values or are discarded, and mainly comprises urban organic solid waste (domestic garbage, municipal sludge, landscaping waste and the like), agricultural organic solid waste (crop straws, livestock and poultry manure and the like), industrial organic solid waste (organic waste residues, automobile dismantling waste and the like), organic hazardous waste, medical waste and the like.

At present, the treatment and disposal modes of organic solid wastes in China mainly comprise sanitary landfill and incineration. With the development of pyrolysis gasification technology, the technology is also gradually applied to the treatment of organic solid wastes. Sanitary landfills are capable of disposing of solid waste at one time, but occupy a large amount of land area and can present some environmental risks over time. The incineration treatment can realize the reduction and the resource of the organic solid waste, but the equipment investment is large, and secondary pollution such as fly ash, dioxin and the like is easily caused. The principle of the gasification incineration technology is that organic solid waste is pyrolyzed in anaerobic or anoxic atmosphere, the heat energy generated by pyrolysis causes the organic matter chemical bond of complex components to be broken, isomerized, polymerized and the like, gas, tar and semicoke are generated in the process, and the semicoke can be gasified to generate combustible gas under the action of a gasifying agent; and the volatile matter further enters a hot blast stove or a secondary combustion chamber along with the flue gas, and the gas-phase and solid-phase products of the organic solid waste are fully combusted in the hot blast stove or the secondary combustion chamber.

The core of the gasification incineration treatment process lies in the selection of the type of the gasification incinerator, the main types of the incinerator at present comprise a grate furnace, a rotary kiln, a fluidized bed, a fixed bed and the like, and different types of the incinerator and gasification incineration methods have conditions and requirements which are adaptive to the different types of the incinerator and gasification incineration methods. The prior art with the patent name of 'a combustible solid waste rotary kiln gasification incineration method' (patent publication number: CN101839488A) discloses a process for gasification combustion of a mixture of oily sludge, municipal sludge, coal gangue, municipal domestic waste and biomass based on a rotary kiln, wherein a series of pretreatment such as mechanical dehydration, crushing, air drying, compatibility and the like is required to be carried out on materials in the process, and a continuous transmission device in the rotary kiln is complex and refractory materials are easy to damage.

SUMMERY OF THE UTILITY MODEL

The present invention aims at solving at least one of the technical problems in the related art to a certain extent. Therefore, the utility model discloses an aim at propose organic solid useless gasification incineration system. The utility model has the main advantages that the gasification furnace main body equipment has simple structure and low requirements on the types and the granularity of raw materials; the middle part of the material layer is extended to discharge gas, so that fly ash and tar in the fuel gas are adsorbed by the material layer in the conveying process, and the content of the fly ash in the fuel gas is low; the preheated air and the steam generated by the waste heat boiler and the gas preheater are used as gasifying agents to return to the gasification furnace, so that the gasification efficiency and the comprehensive heat utilization efficiency are improved.

The utility model provides an organic solid useless gasification system of burning. According to the embodiment of the utility model, this organic solid useless gasification system of burning includes: the system comprises a fixed bed gasification furnace, a secondary combustion chamber, a waste heat boiler and a gas preheater;

the fixed bed gasification furnace comprises a feeding device, a reaction zone furnace body, a furnace top gasifying agent air inlet, a middle section gasifying agent air inlet, a furnace bottom gasifying agent air inlet, a coal gas air outlet and a slag discharging device;

the reaction zone furnace body is arranged below the feeding device and comprises an upper section furnace body and a lower section furnace body, the outer diameter of the upper section furnace body is smaller than the inner diameter of the lower section furnace body, the upper section furnace body is partially sleeved in the lower section furnace body, an epitaxial annular cavity is formed by the overlapped part of the upper section furnace body and the lower section furnace body, and a sealing element is arranged at the top of the epitaxial annular cavity; a grate is arranged at the bottom in the lower section furnace body;

the furnace top gasification agent gas inlet is arranged on the top and/or the upper part of the upper-section furnace body and extends into the upper-section furnace body;

the middle-section gasifying agent air inlet is arranged below the furnace top gasifying agent air inlet, is arranged on the side wall of the upper-section furnace body and extends into the upper-section furnace body;

the furnace bottom gasification agent air inlet is communicated with the lower part of the grate;

the gas outlet is arranged on the side wall of the lower furnace body corresponding to the epitaxial annular cavity and is communicated with the epitaxial annular cavity;

the slag discharging device is arranged below or laterally below the lower furnace body;

the secondary combustion chamber is provided with a coal gas inlet and a high-temperature flue gas outlet, and the coal gas inlet is connected with the coal gas outlet;

the waste heat boiler is provided with a high-temperature flue gas inlet, a superheated steam outlet and a cooling flue gas outlet, the high-temperature flue gas inlet is connected with the high-temperature flue gas outlet, and the superheated steam outlet is connected with the air inlet of the fixed bed gasification furnace;

the gas preheater is provided with a cooling flue gas inlet, a cold gas inlet, a preheating gas outlet and a tail gas outlet, wherein the cooling flue gas inlet is connected with the cooling flue gas outlet, and the preheating gas outlet is connected with the gas inlet of the fixed bed gasification furnace.

According to the organic solid waste gasification incineration system of the embodiment of the utility model, 1) through the arrangement of the furnace top gasifying agent air inlet, the middle section gasifying agent air inlet and the furnace bottom gasifying agent air inlet, the multistage supply of the gasifying agent can be realized, and further the stable control of the oxidation layer can be realized through the accurate and stable multistage oxidation, so that the tar in the fuel gas is fully cracked, thereby not only improving the quality of the obtained coal gas, but also ensuring the lower carbon content of the ash residue; 2) the gasification requirements of the carbon-containing organic solids with different volatile matter contents and fixed carbon contents can be met by adjusting the supply amount of the gasification agent at different positions and the position of the middle section gasification agent air inlet; 3) the epitaxial gas outlet mode is adopted, so that high-temperature area components in the furnace are reduced, the slagging problem is avoided, and meanwhile, the vertical upward epitaxial annular cavity can effectively reduce particles in the gas; 4) the gas flowing mode of the upper section concurrent flow and the lower section countercurrent flow can avoid the environmental pollution caused by the gas leakage at the top feed inlet of the traditional countercurrent gasification furnace; 5) compared with the rotary kiln, the fluidized bed, the grate furnace pyrolysis gasifier and the like in the prior art, the fixed bed gasifier of the utility model has the advantages of simple equipment structure, low requirements on the types and the granularity of raw materials and the like; 6) compared with the direct gasification incineration in the prior art, the utility model separates the gasification process of organic solid waste from the gas incineration process, can control the generation of tar in the gasification process, effectively avoids the environmental hazard caused by the direct combustion of tar, and reduces the cost of the subsequent flue gas treatment; 7) high-temperature flue gas generated by combustion of fuel gas in the secondary combustion chamber is subjected to waste heat recovery in a waste heat boiler, and generated water vapor is returned to the gasification furnace to be used as a gasification agent, so that the preparation cost of hot air and water vapor is reduced; 8) the flue gas that will pass through waste heat boiler preliminary cooling is supplied with to gas heater, and the flue gas of preliminary cooling carries out the heat exchange with the cold gas and makes the cold gas become preheating gas, and preheating gas returns to the gasifier to gasification efficiency and heat comprehensive utilization efficiency have effectively been improved.

In addition, according to the utility model discloses above-mentioned organic solid useless gasification system of burning of embodiment can also have following additional technical characterstic:

in some embodiments of the present invention, the feeding device comprises at least one feeding channel, each feeding channel is sequentially provided with a feeding port, an upper valve of a feeding buffer bin, a lower valve of the feeding buffer bin and an inert gas purging air inlet from top to bottom, and a side portion of the feeding buffer bin is provided with a feeding buffer bin pressure charging and discharging port; the top of the upper-section furnace body is connected with the feeding device through a transition bin, the transition bin is communicated with a furnace chamber of the reaction zone furnace body, and a furnace top gasification agent air inlet is arranged on the side wall of the transition bin. Therefore, the safety of the operation of the gasification furnace can be effectively ensured by the design of the inert gas purging air inlet and the charging and discharging pressure of the feeding buffer bin.

In some embodiments of the present invention, the feeding device comprises two feeding channels, and a communicating valve is disposed between the feeding buffer bins of the two feeding channels; and the discharge end of the feeding channel is communicated with the transition bin and is positioned above the furnace top gasifying agent air inlet.

In some embodiments of the utility model, arrange sediment device from top to bottom include in proper order on the sediment storehouse valve, sediment storehouse lower valve the lateral part in sediment storehouse is equipped with sediment storehouse and fills the pressure release mouth.

The utility model discloses an in some embodiments, the lower part of hypomere furnace body is the back taper, the bottom of hypomere furnace body is equipped with the slag notch, arrange the sediment device and establish the below of hypomere furnace body, and with the slag notch links to each other.

In some embodiments of the utility model, the lower part lateral wall of hypomere furnace body is equipped with the slag notch, arrange the sediment device and establish the side below of hypomere furnace body, and with the slag notch links to each other.

In some embodiments of the present invention, the grate is rotatably disposed, and the grate is formed with a cloth opening.

The utility model discloses an in some embodiments, arrange the sediment device and set up in aqueous and be located the below of reaction zone furnace body, arrange the sediment device and include ash tray, disintegrating slag circle, grate support piece and first ash sword, the ash tray sets up the below of grate, the disintegrating slag circle is cyclic annular and the cover is established in the ash tray, grate support piece sets up the below of grate just is located in the disintegrating slag circle, first ash sword sets up on the inside wall of ash tray. From this, the ash tray water seal is constituteed jointly with the disintegrating slag circle to the ash tray, because there is certain pressure in the stove, extrudees the water in the ash tray to take the altitude and realize having the pressure liquid seal, thereby gas can emerge safe pressure release from the aquatic when the stove internal pressure is too big, thereby the mode that adopts ash tray liquid seal wet process to arrange the sediment can effectual control the malleation state in the stove, reduces the potential safety hazard of gasifier.

In some embodiments of the present invention, the slag discharging device further comprises a second ash knife and a slag breaking block, the second ash knife is disposed at the bottom of the grate support member, and the slag breaking block is disposed on the side wall of the grate support member.

In some embodiments of the present invention, the grate is rotatably disposed, and the grate is formed with the air distribution openings, and the grate support is used for supporting the grate and rotating with the grate.

In some embodiments of the present invention, the gasification furnace further comprises a distribution regulator of gasification agent, the distribution regulator of gasification agent can be disposed at the outlet end of the air inlet of the gasification agent at the bottom of the furnace and can move up and down, and is located in the grate. Therefore, the gasification agent distribution regulator can better adapt to the uniform gas distribution under the condition of small flow of the gasification agent inlet at the bottom of the furnace.

In some embodiments of the present invention, the gasification furnace further comprises a material distribution device, and the material distribution device is disposed above the upper section of the furnace body. From this, the distributing device can realize the even cloth of material in the dry layer better.

In some embodiments of the present invention, the top gasifier air inlet is a plurality of, a plurality of the top gasifier air inlets are arranged along the circumferential symmetry of the reaction zone furnace body.

In some embodiments of the present invention, the middle-stage gasifying agent inlet is a plurality of inlets, and a plurality of inlets are arranged along the circumferential symmetry of the reaction zone furnace body.

In some embodiments of the present invention, the height of the epitaxial annular cavity is 10% to 30% of the total height of the reaction zone furnace body.

In some embodiments of the present invention, the ratio of the width of the epitaxial annular cavity to the inner diameter of the reaction zone furnace body is (0.1-0.3): 1.

In some embodiments of the present invention, the inner diameter of the upper furnace body is 0.3-8.0 m, and the inner diameter of the lower furnace body is 0.4-8.0 m.

In some embodiments of the present invention, the height of the upper furnace body is 40% -80% of the total height of the reaction zone furnace body.

In some embodiments of the present invention, the height of the upper furnace body from the grate is 20% -60% of the total height of the reaction zone furnace body. Therefore, carbon dioxide generated by the oxidation layer reacts with the carbon layer of the reduction section to generate required carbon monoxide, and the distance between the upper-section furnace body and the grate is set to be within the range, so that the carbon dioxide and the carbon layer have reasonable reaction contact time.

In some embodiments of the present invention, the second combustion chamber further has an induced draft fan inlet disposed at a lower portion of the gas inlet for supplying the induced draft fan with the combustion improver.

In some embodiments of the present invention, the gas preheater is a box-type tube array structure, the cooling flue gas passes through the tube pass, and the cool air passes through the shell pass.

In some embodiments of the present invention, an air release valve is disposed above the gas preheater.

In some embodiments of the present invention, the outer sides of the upper furnace body and the lower furnace body are membrane water walls or jacket water walls. Therefore, the membrane type water-cooled wall reduces the outward radiation heat of the furnace body, effectively avoids the slag bonding phenomenon caused by high temperature in the furnace, also reduces the gas temperature of the gas outlet, and can effectively avoid the safety problem of jacket explosion caused by bulging compared with the traditional mode of adopting a water jacket.

In some embodiments of the present invention, the membrane wall is a shell and tube membrane wall or a coil membrane wall.

Additional aspects and advantages of the invention will be set forth in part in the description which follows and, in part, will be obvious from the description, or may be learned by practice of the invention.

Drawings

The above and/or additional aspects and advantages of the present invention will become apparent and readily appreciated from the following description of the embodiments, taken in conjunction with the accompanying drawings of which:

fig. 1 is a schematic structural view of a fixed-bed gasification furnace according to embodiment 1 of the present invention.

Fig. 2 is a front view of a slag discharge apparatus in a fixed-bed gasification furnace according to embodiment 1 of the present invention.

Fig. 3 is a plan view of a slag discharge apparatus in a fixed-bed gasification furnace according to embodiment 1 of the present invention.

Fig. 4 is a schematic structural view of a fixed-bed gasification furnace according to embodiment 2 of the present invention.

Fig. 5 is a schematic structural view of a fixed-bed gasification furnace according to embodiment 3 of the present invention.

Fig. 6 is a schematic structural diagram of an organic solid waste gasification incineration system according to embodiment 4 of the present invention.

Detailed Description

Reference will now be made in detail to embodiments of the present invention, examples of which are illustrated in the accompanying drawings, wherein like reference numerals refer to the same or similar elements or elements having the same or similar function throughout. The embodiments described below with reference to the drawings are exemplary and intended to be used for explaining the present invention, and should not be construed as limiting the present invention.

In the description of the present invention, it is to be understood that the terms "center", "longitudinal", "lateral", "length", "width", "thickness", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", "axial", "radial", "circumferential", and the like indicate orientations or positional relationships based on those shown in the drawings, and are only for convenience of description and simplicity of description, and do not indicate or imply that the device or element referred to must have a particular orientation, be constructed and operated in a particular orientation, and therefore should not be construed as limiting the present invention.

Furthermore, the terms "first", "second" and "first" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defined as "first" or "second" may explicitly or implicitly include at least one such feature. In the description of the present invention, "a plurality" means at least two, e.g., two, three, etc., unless specifically limited otherwise.

In the present invention, unless otherwise expressly specified or limited, the terms "mounted," "connected," "secured," and the like are to be construed broadly, e.g., as meaning permanently connected, detachably connected, or integral to one another; can be mechanically or electrically connected; they may be directly connected or indirectly connected through intervening media, or they may be connected internally or in any other suitable relationship, unless expressly stated otherwise. The specific meaning of the above terms in the present invention can be understood according to specific situations by those skilled in the art.

In the present application, unless expressly stated or limited otherwise, the first feature may be directly on or directly under the second feature or indirectly via intermediate members. Also, a first feature "on," "over," and "above" a second feature may be directly or diagonally above the second feature, or may simply indicate that the first feature is at a higher level than the second feature. A first feature being "under," "below," and "beneath" a second feature may be directly under or obliquely under the first feature, or may simply mean that the first feature is at a lesser elevation than the second feature.

The utility model provides an organic solid useless gasification system of burning, the system includes fixed bed gasifier, second combustion chamber, exhaust-heat boiler and gas heater. According to the utility model discloses an embodiment, the fixed bed gasifier includes feed arrangement, reaction zone furnace body, top of a furnace gasification agent air inlet, middle section gasification agent air inlet, stove bottom gasification agent air inlet, coal gas outlet and arranges the sediment device.

According to the utility model discloses an embodiment, feed arrangement is used for supplying with organic solid useless to the reaction zone furnace body. The feeding device can comprise at least one feeding channel, each feeding channel is sequentially provided with a feeding hole, an upper valve of a feeding buffer bin, a lower valve of the feeding buffer bin and an inert gas purging air inlet from top to bottom, and a charging and pressure releasing port of the feeding buffer bin is formed in the side part of the feeding buffer bin; the feeding device comprises a feeding device, a feeding buffer bin, an inert gas purging inlet, a feeding buffer bin pressure relief opening, a buffer bin pressure relief opening and a reaction zone furnace body, wherein the feeding device is arranged in the feeding device, the feeding device is provided with the inert gas purging inlet, the feeding buffer bin pressure relief opening is provided with the inert gas purging inlet, and the inert gas purging inlet is used for purging the inert gas to the lower part of the feeding device; in addition, the upper valve of the feeding buffer bin and the lower valve of the feeding buffer bin can be alternately used, when organic solid waste enters the feeding buffer bin, the upper valve of the feeding buffer bin can be opened, and the lower valve of the feeding buffer bin is closed; when organic solid waste in the feeding buffer bin is supplied to a furnace chamber of the reaction zone furnace body, the upper valve of the feeding buffer bin can be closed, and the lower valve of the feeding buffer bin is opened.

According to the utility model discloses a concrete embodiment, in single channel feed arrangement, the feed inlet can be for narrow conical feed inlet down wide, and the welding of lower part has circular flange. The feed inlet lower part is the feeding surge bin upper valve, connect through the flange, the feeding surge bin upper valve lower part furnace body is the feeding surge bin, the feeding surge bin lower part is feeding surge bin lower valve, the feeding surge bin upper valve, the feeding surge bin, pass through flange joint between the feeding surge bin lower valve, the feeding surge bin is narrow wide cylindrical structure in the middle of from top to bottom, the feeding surge bin side is equipped with the feeding surge bin and fills the pressure release mouth, the feeding surge bin fills the pressure release mouth horizontal arrangement.

According to another embodiment of the present invention, the utility model finds that the gasification furnace can improve gasification intensity and gasification efficiency by a pressurized gasification method, but the handling capacity of the material in unit time is limited by the diameter of the valve of the feeding port and intermittent pressure charging and discharging, and the lifting of the handling capacity can not be realized, and simultaneously, a large amount of dust-containing flue gas can be discharged through the pressure charging and discharging port in the single-channel feeding and pressure charging and discharging process, therefore, the feeding device can be optimized to comprise two feeding channels a and b, a communicating valve can be arranged between the feeding buffer bins of the two feeding channels a and b, in the double-channel feeding device, the number of the feeding buffer bins is two, the corresponding upper valve of the feeding buffer bin, the lower valve of the feeding buffer bin and the inert gas purging air inlet are two, two conical discharge ports are arranged at the bottom of the feeding port, and are respectively connected with the upper valves of the two feeding buffer bins through flanges, the lower part of the lower valve of the feeding buffer bin is provided with the feeding buffer bin which is connected through a flange, and a feeding buffer bin gas channel is arranged between the feeding buffer bins and is controlled to be opened and closed through a communicating valve; the side edges of the two feeding buffer bins are respectively provided with a feeding buffer bin pressure charging and releasing port; the lower part of the feeding buffer bin is connected with a lower valve of the feeding buffer bin through a flange; the lower valve of the feeding buffer bin is a channel connected into the transition bin, and the inert gas purging air inlet is positioned on the channel at the lower part of the lower valve of the feeding buffer bin and horizontally arranged. Through the combination use of feeding surge bin upper valve, feeding surge bin lower valve in intercommunication valve and two feed channel, not only can solve the single channel feeding and fill the problem that the pressure release process can bring a large amount of dusty flue gas, can also improve the organic solid useless supply volume of supplying to in the furnace chamber in the unit interval, solve the limited problem of feeding volume.

According to the embodiment of the utility model, the reaction zone furnace body is arranged below the feeding device, the reaction zone furnace body comprises an upper section furnace body and a lower section furnace body, the outer diameter of the upper section furnace body is smaller than the inner diameter of the lower section furnace body, the upper section furnace body is partially sleeved in the lower section furnace body, the superposed part of the upper section furnace body and the lower section furnace body forms an epitaxial annular cavity, and the top of the epitaxial annular cavity is provided with a sealing element; the bottom in the lower section furnace body is provided with a grate. The furnace top gasification agent gas inlet is arranged on the top and/or the upper part of the upper-section furnace body and extends into the upper-section furnace body; the middle-section gasifying agent air inlet is arranged below the furnace top gasifying agent air inlet, is arranged on the side wall of the upper-section furnace body and extends into the upper-section furnace body; the furnace bottom gasification agent air inlet is communicated with the lower part of the grate; the gas outlet is arranged on the side wall of the lower furnace body corresponding to the epitaxial annular cavity and communicated with the epitaxial annular cavity. Therefore, by arranging the furnace top gasifying agent air inlet, the middle section gasifying agent air inlet and the furnace bottom gasifying agent air inlet, the multistage supply of the gasifying agent can be realized, and then the stable control of the oxidation layer can be realized by accurate and stable multistage oxidation, so that tar in the fuel gas is fully cracked, the quality of the obtained coal gas is improved, and the lower carbon content of ash slag is ensured. Meanwhile, the gasification requirements of the carbon-containing organic solids with different volatile matter contents and fixed carbon contents can be met by adjusting the supply amount of the gasification agent at different positions and the position of the middle section gasification agent air inlet. In addition, the mode of epitaxial gas outlet is adopted to reduce high-temperature zone components in the furnace, the slagging problem is avoided, and meanwhile, the vertical upward epitaxial annular cavity can effectively reduce particles in the gas. And the gas flowing mode of the upper section concurrent flow and the lower section countercurrent flow can avoid the environmental pollution caused by the gas leakage at the top feed inlet of the traditional countercurrent gasification furnace.

According to the utility model discloses a part that hypomere furnace body internal diameter surpassed upper segment furnace body external diameter is provided with epitaxial toroidal cavity and coal gas outlet, and epitaxial toroidal cavity is located that upper segment furnace body membrane water-cooling wall is outer to surpass upper segment furnace body top region with hypomere furnace body internal diameter, and epitaxial toroidal cavity adopts resistant firebrick material to insulate against heat outward, and the coal gas outlet is located epitaxial toroidal cavity top level and places.

According to the utility model discloses an embodiment can utilize furnace roof gasification agent air inlet, middle section gasification agent air inlet and stove bottom gasification agent air inlet to supply with the gasification agent to the reaction zone furnace body, divide into drying layer, dry distillation layer, last oxide layer, reduction layer, oxide layer and ash residue layer with the reaction zone furnace body from top to bottom, makes organic solid useless gasification reaction that takes place, obtains combustible gas and lime-ash, and combustible gas passes through coal gas outlet discharge reaction zone furnace body, and wherein, combustible gas can be for coal gas.

According to the utility model discloses a specific embodiment, furnace top gasification agent air inlet 6 is a plurality of, and is a plurality of the furnace top gasification agent air inlet is followed the circumference level of reaction zone furnace body is evenly arranged. Therefore, the plurality of furnace top gasifying agent air inlets are uniformly arranged in an annular mode, and uniform air distribution is realized through the plurality of furnace top gasifying agent air inlets and the cavity area in the furnace top.

According to the utility model discloses a still another embodiment, the middle section gasification agent air inlet is a plurality of, and is a plurality of the middle section gasification agent air inlet is followed the circumference symmetry of reaction zone furnace body sets up, realizes even cloth wind from this.

According to the utility model discloses an embodiment, stove bottom gasification agent air inlet with the lower part of grate intercommunication. The air inlet of the furnace bottom gasification agent is connected with an external air source through a pipeline positioned below the furnace bottom gasification agent, air distribution ports are distributed on the furnace grate to realize the uniform air distribution of the air inlet of the furnace bottom, and the introduced air is water vapor, carbon dioxide, air, oxygen enrichment (the oxygen concentration is 21-100 percent) and mixed gas of the four gases in different proportions.

The height of the epitaxial annular cavity is 10% -30% of the total height of the furnace body of the reaction zone, so that the epitaxial annular cavity can be guaranteed to have enough height, the combustible gas product can be further cooled, sufficient settling space is provided for particles in the combustible gas, and the particles in the combustible gas are reduced.

The embodiment of the utility model provides an in, the specific numerical value of the internal diameter of above-mentioned upper segment furnace body and hypomere furnace body is not restricted by specially, and the personnel in the field can select at will according to actual conditions, as an optimal scheme, the internal diameter of upper segment furnace body is 0.3 ~ 8.0m, the internal diameter of hypomere furnace body is 0.4 ~ 8.0 m.

According to a specific embodiment of the present invention, the ratio of the width of the epitaxial annular cavity to the inner diameter of the reaction zone furnace body is (0.1-0.3): 1, such as 0.1:1, 0.2:1, 0.3:1, etc. The utility model discloses the people discovers, if the width of epitaxial toroidal cavity is too big, can reduce the reaction space in the stove, lead to gasifier throughput to show and reduce, and if the width undersize of epitaxial toroidal cavity, neither do benefit to subsiding of particulate matter, also do not benefit to the staff and overhaul to epitaxial toroidal cavity, and be above-mentioned width scope through controlling epitaxial toroidal cavity, can compromise the throughput of gasifier and the effect of subsiding of particulate matter in the gas simultaneously, the lime-ash come-up influences the problem of gas quality when avoiding appearing because of the gas flow is great, still be convenient for realize the installation and the maintenance of epitaxial toroidal cavity. The width of the epitaxial ring cavity refers to the width of the single-sided epitaxial ring cavity in the horizontal direction.

According to another embodiment of the present invention, the height of the upper furnace body is 40% -80% of the total height of the reaction zone furnace body, such as 40%, 60%, 80%, etc. Therefore, macromolecular organic matters generated by cracking high-volatile materials have long retention time in a higher material layer, the probability of cracking the macromolecular organic matters into inorganic micromolecules is improved, tar in coal gas is reduced to the maximum extent, and the cleanness degree of the coal gas is improved.

According to the utility model discloses a still another embodiment, the upper segment furnace body is apart from the height of grate does 20% ~ 60%, for example 20%, 40%, 60% etc. of reaction zone furnace body total height, from this, makes the carbon dioxide that the oxide layer produced and the carbon layer reaction of reduction section generate required carbon monoxide, and the distance between upper segment furnace body and the grate sets up to above-mentioned scope, can make carbon dioxide and carbon layer have reasonable reaction contact time.

According to the utility model discloses a still another embodiment, the upper segment furnace body with the outside of hypomere furnace body is the membrane wall, the membrane wall can be for shell and tube or coil type, also can replace for the water jacket. The upper furnace body, the lower furnace body and the membrane water-cooled wall are fixed through flanges. Therefore, the membrane type water-cooled wall reduces the outward radiation heat of the furnace body, effectively avoids the slag bonding phenomenon caused by high temperature in the furnace, also reduces the gas temperature of the gas outlet, and can effectively avoid the bulge problem compared with the traditional mode of adopting a water jacket.

According to the utility model discloses an embodiment, arrange the sediment device and can establish in the below or the side below of reaction zone furnace body for arrange sediment or the mode of arranging the sediment with lime-ash discharge reaction zone furnace body through the center, arrange the below that the sediment device also can set up in aqueous and be located the reaction zone furnace body.

According to the utility model discloses an embodiment, the grate can be rotatable setting, can be formed with the cloth wind mouth on the grate, can further realize the even cloth wind of stove bottom air inlet from this.

According to a specific embodiment of the utility model, the lower end of the grate is provided with a furnace bottom gasification agent air inlet which is communicated with the grate, an ash discharge channel is arranged right below or laterally below the grate, and the furnace bottom gasification agent air inlet is connected with an external air source through a pipeline positioned right below or laterally below the grate; the grate can be welded with a scraper to crush ash, gas distribution ports are distributed on the grate to realize uniform gas distribution of the furnace bottom gasification agent, and the introduced gasification agent is water vapor, carbon dioxide, air, oxygen enrichment (oxygen concentration is 21-100 v%) and mixed gas of the four gases in different proportions.

According to the utility model discloses a concrete embodiment, arrange the sediment mode and can arrange the sediment for the center, the lower part of hypomere furnace body can be the back taper structure this moment, the region that corresponds with the grate on the hypomere furnace body can be equipped with the scraper that is used for broken lime-ash, the bottom of back taper structure is formed with the slag notch, the slag notch links to each other with row's sediment device, therefore, the grate can drive rotatoryly through the motor, the slag of top ash layer is realized the breakage of slag by the scraper, avoid massive slag to block up, the slag gets into row's sediment device under the action of gravity along the center slag notch of grate below at the center of below after the grate is broken.

According to the utility model discloses a still another embodiment, arrange the sediment mode and can be for the side row sediment, can be equipped with the scraper that is used for broken lime-ash on the grate, can be formed with the slag notch on the lateral wall of hypomere furnace body lower part, and the slag notch links to each other with row's sediment device. From this, grate accessible motor drives rotatoryly, and the scraper that has on the grate can realize the breakage of slag, avoids massive slag to block up, and the cinder notch through the side gets into the sediment device through rotatory extrusion after the ash residue is broken by the grate.

According to the utility model discloses a still another embodiment, arrange sediment device and can include valve, sediment storehouse and sediment storehouse lower valve on the sediment storehouse in proper order from top to bottom, the lateral part in sediment storehouse can be equipped with the sediment storehouse and fill the pressure release mouth. Wherein, the reactor furnace body slag notch below is valve on the sediment storehouse, and the furnace body bottom passes through flange joint with the sediment storehouse, goes up through flange joint between valve and the sediment storehouse in the sediment storehouse, and the sediment storehouse is narrow wide cylindrical structure in the middle of from top to bottom for collect the lime-ash, the sediment storehouse is down the valve and passes through flange joint with the sediment storehouse.

According to the utility model discloses a sediment mode can be arranged for the wet process sediment again, and the fire grate off-centre is arranged on the ash pan, and the ash pan constitutes the ash pan water seal jointly with the disintegrating slag circle, and the welding of ash knife is circled at furnace body and disintegrating slag in addition simultaneously, and rotatory process is broken and is arranged the sediment to the lime-ash. Specifically, referring to fig. 2 and 3, the slag discharging device is arranged in water and located below the lower furnace body, the slag discharging device includes ash trays 1-13, slag breaking rings 1-19, grate supporting members 1-21 and first ash knives 1-20, the ash trays 1-13 are arranged below the grates 1-12, the slag breaking rings 1-19 are welded together with the upper membrane wall in an annular shape and sleeved in the ash trays 1-13, the grate supporting members 1-21 are arranged below the grates 1-12 and located in the slag breaking rings 1-19, the first ash knives 1-20 are arranged on the inner side wall of the ash trays, and the first ash knives 1-20 are in a plough shape. Further, referring to fig. 2 and 3, the slag discharging device further includes a second ash knife 1-22 and a clinker 1-23, the second ash knife 1-22 is disposed at the bottom of the grate support 1-21, and the clinker 1-23 is disposed on the side wall of the grate support 1-21, thereby better crushing the clinker. It should be noted that the first plaster cutter refers to a large plaster cutter, and the second plaster cutter refers to a small plaster cutter. Specifically, ash is discharged from the reaction zone furnace body and enters an ash tray 1-13, the ash in the ash tray 1-13 is crushed along with the rotation of the grate support 1-21 under the extrusion action of the slag crushing ring 1-19, the grate support 1-21, the second ash knife 1-22 and the slag crushing block 1-23, and the crushed ash is discharged from the ash tray along the direction of the first ash knife. From this, the ash tray water seal is constituteed jointly with the disintegrating slag circle to the ash tray, because there is certain pressure in the stove, extrudees the water in the ash tray to take the altitude and realize having the pressure liquid seal, thereby gas can emerge safe pressure release from the aquatic when the stove internal pressure is too big, thereby the mode that adopts ash tray liquid seal wet process to arrange the sediment can effectual control the malleation state in the stove, reduces the potential safety hazard of gasifier.

Furthermore, the gasifier still includes gasification agent distribution regulator, gasification agent distribution regulator can set up with reciprocating the exit end of stove bottom gasification agent air inlet, and is located in the grate, adjust the distribution of gasification agent in the grate through reciprocating of gasification agent distribution regulator, adapt to the even gas distribution under the little flow condition of stove bottom gasification agent air inlet better.

Further, the gasification furnace also comprises a material distribution device, and the material distribution device is arranged above the upper section of the furnace body. From this, the distributing device realizes the even cloth of material in the dry layer.

According to the utility model discloses an embodiment, two combustion chambers have coal gas air inlet and high temperature exhanst gas outlet, the coal gas air inlet with the coal gas outlet links to each other. The secondary combustion chamber is also called as an incinerator or a hot blast stove, and aims to introduce fuel gas obtained after organic solid waste gasification into the secondary combustion chamber for combustion to generate heat and hot flue gas for subsequent processes. Specifically, the second combustion chamber is of a cylinder structure, and refractory bricks are lined in the furnace. The secondary combustion chamber is also provided with an induced draft fan inlet arranged at the lower part of the coal gas inlet, the induced draft fan inlet is connected with the induced draft fan (namely a combustion-supporting air blower), and the induced draft fan can supplement combustion improver (air or oxygen) into the secondary combustion chamber when the heat value of the fuel gas is insufficient.

According to the utility model discloses an embodiment, exhaust-heat boiler has high temperature gas inlet, superheated steam export and cooling exhanst gas outlet, high temperature gas inlet with high temperature exhanst gas outlet links to each other, superheated steam export with the air inlet of fixed bed gasifier links to each other. Specifically, the waste heat boiler comprises a superheater, an evaporator, an economizer and a steam drum in a hearth, and high-temperature flue gas sequentially passes through the superheater, the evaporator, the economizer and the steam drum in the hearth; the water absorbs heat in the economizer, the temperature rises to a saturation temperature slightly lower than the pressure of the steam pocket, the water enters the steam pocket, the water entering the steam pocket is mixed with saturated water in the steam pocket and then enters the evaporator along the downcomer to start steam generation, the steam-water mixture enters the steam pocket through the riser to be subjected to steam-water separation, the water enters the downcomer in the water space in the steam pocket to continuously absorb heat to generate steam, and the steam enters the superheater from the upper part of the steam pocket to enable the saturated steam to be changed into superheated steam. The specific structure of the waste heat boiler belongs to the common knowledge in the field and is not described in detail herein.

According to the utility model discloses an embodiment, gas preheater has cooling gas inlet, cold gas import, preheats gas outlet and tail gas outlet, cooling gas inlet with cooling gas outlet links to each other, preheat gas outlet with the air inlet of fixed bed gasifier links to each other. Furthermore, the gas preheater is of a box type tube array structure, the cooling flue gas after waste heat recovery of the waste heat boiler passes through a tube pass, the cold gas enters a shell pass of the gas preheater through a gas blower, and after heat exchange is carried out between the flue gas and the cold gas, the preheated gas is conveyed to the gasification furnace along with a pipeline. Further, an air escape valve is arranged above the gas preheater, and air in the shell side is released emergently when the air or hot air is overloaded or the temperature is too high.

Compared with the prior art, the utility model discloses organic solid useless gasification system of burning has the advantage mainly to be reflected in: 1) the multi-stage supply of the gasifying agent is realized through the top gas inlet, the middle section gasifying agent gas inlet and the bottom gasifying agent gas inlet, and the stable control of an oxidation layer is realized through accurate and stable multi-stage oxidation, so that tar in fuel gas is fully cracked, the quality of combustible gas is improved, and the lower carbon content of slag is ensured; 2) the gasification requirements of carbon-containing organic solids with different volatile matter contents and fixed carbon contents can be met by adjusting the supply amount of the gasification agent at different positions and the position of the gas inlet of the middle-section gasification agent; 3) the gasification agent distribution regulator can better adapt to uniform gas distribution under the condition of small flow of a gasification agent inlet at the bottom of the furnace; 4) the gas leakage of a top feed port can be avoided by the gas flow mode of the forward flow of the upper section and the reverse flow of the lower section, the high-temperature area components in the furnace are reduced by adopting the epitaxial gas outlet mode, the slagging problem is avoided, and meanwhile, the particles in the gas can be reduced by the vertically upward epitaxial annular cavity; 5) the furnace is under the condition of positive pressure reaction, compared with the negative pressure state, the gasification reaction rate is higher, and the treatment capacity of the gasification furnace is larger; 6) the positive pressure state in the furnace can be effectively controlled by adopting an ash tray liquid seal wet-method slag discharge mode, and the potential safety hazard of the gasification furnace is reduced; 7) the membrane type water-cooled wall is used for cooling the furnace body, so that the operation is more stable, and the swelling phenomenon of a water jacket is avoided; 8) the safety of the operation of the gasification furnace can be effectively ensured by the aid of the design of the blowing air inlet, the charging buffer bin and the slag bin; 9) compared with the direct gasification incineration in the prior art, the utility model separates the gasification process of organic solid waste from the gas incineration process, can control the generation of tar in the gasification process, effectively avoids the environmental hazard caused by the direct combustion of tar, and reduces the cost of the subsequent flue gas treatment; 10) high-temperature flue gas generated by combustion of fuel gas in the secondary combustion chamber is subjected to waste heat recovery in a waste heat boiler, and generated water vapor is returned to the gasification furnace to be used as a gasification agent, so that the preparation cost of hot air and water vapor is reduced; 11) the flue gas that will pass through waste heat boiler preliminary cooling is supplied with to gas heater, and the flue gas of preliminary cooling carries out the heat exchange with the cold gas and makes the cold gas become preheating gas, and preheating gas returns to the gasifier to gasification efficiency and heat comprehensive utilization efficiency have effectively been improved.

For convenience of understanding, a method for gasification incineration of organic solid waste using the gasification incineration system for organic solid waste of the above embodiment is described in detail below, and the method comprises the following steps:

(1) organic solid waste is supplied to the furnace body of the reaction area through the feeding device, and inert protective gas is blown to the lower part of the feeding device through the inert gas blowing inlet.

(2) And the gasification agent is supplied to the reaction zone furnace body through a furnace top gasification agent air inlet, a middle section gasification agent air inlet and a furnace bottom gasification agent air inlet, and the reaction zone furnace body comprises a drying layer, a dry distillation layer, an upper oxidation layer, a reduction layer, a lower oxidation layer and an ash residue layer which are sequentially arranged from top to bottom.

In this step, a gasifying agent is fed into the furnace by a blower to bring the pressure inside the furnace into a positive pressure state, the pressure inside the reaction zone furnace body is 0 to 20.0kPa (for example, 0.1kPa, 1kPa, 4kPa, 8kPa, 12kPa, 14kPa, 20kPa, etc.), the gasifying agent pressure at the gas inlet is 0 to 20kPa, and the pressure is a gauge pressure measured by a pressure gauge. Therefore, the positive pressure state is maintained in the control furnace, potential safety hazards in the negative pressure operation process are avoided, and meanwhile, compared with the negative pressure state, the gasification reaction rate is higher and the gasifier treatment capacity is larger when the positive pressure reaction condition exists in the furnace.

Further, the gasifying agent includes at least one of water vapor, carbon dioxide, air, and oxygen-rich gas (oxygen concentration 21 v% to 100 v%).

Further, the gasifying agent is a mixed gas of water vapor and oxygen-enriched air, and the ratio of the mass of the water vapor to the volume of the oxygen in the oxygen-enriched air is 0-8.0 kg/Nm³For example 0.1kg/Nm³、1.0kg/Nm³、3.0kg/Nm³、5.0kg/Nm³、7.0kg/Nm³、8.0kg/Nm³And the like. The utility model discloses the people discovery, when the gas mixture of vapor and oxygen boosting is adopted to the gasification agent, through the quality of control vapor and the volume ratio of oxygen in the oxygen boosting in above-mentioned scope, can make the material gasification temperature of different ash fusion points maintain below the softening point temperature of lime-ash, prevent that the lime-ash slagging scorification from influencing gasifier normal operating. Preferably, the ratio of the mass of the water vapor to the volume of the oxygen in the oxygen-enriched air is set to 1.0 to 6.0kg/Nm³. If the ratio of the mass of the water vapor to the volume of the oxygen in the rich oxygen is too large, the gasification reaction temperature may be reduced, which causes the content of the effective components such as carbon monoxide and hydrogen in the coal gas to be reduced, and the heat value of the coal gas to be reduced. If the ratio of the mass of the steam to the volume of the oxygen in the rich oxygen is too small, the gasification reaction temperature may be raised to make the temperature of the oxidation layer higher than the softening point temperature of the ash, so that the ash slagging gasification furnace cannot normally operate.

Further, the gasifying agent is a mixed gas of steam and air, and the temperature of the gasifying agent is 40-70 ℃, such as 40 ℃, 50 ℃, 60 ℃, 70 ℃ and the like. The utility model discloses the people discovery, when the gas mixture of vapor and air is adopted to the gasifying agent, through the temperature of control gasifying agent in above-mentioned scope, can make the air bring into the water gas reaction that the oxidation reduction layer that proper amount vapor got into the gasifier takes place carbon and vapor, generates carbon monoxide and hydrogen. If the temperature of the gasifying agent is too low, the amount of water vapor possibly brought in is less, so that the temperature of an oxidation layer is too high, and if the temperature of the oxidation layer is higher than the softening point temperature of ash, serious slagging phenomenon can be caused, and the normal operation of the gasification furnace is influenced; if the temperature of the gasifying agent is too high, the amount of water vapor possibly brought in is too high, and the reaction temperature is too low, so that the quality of the coal gas is reduced.

Further, the gasifying agent is a mixed gas of carbon dioxide and oxygen-enriched air, and the ratio of the mass of the carbon dioxide to the volume of oxygen in the oxygen-enriched air is 0-19.5 kg/Nm³E.g. 0.10kg/Nm³、1.0kg/Nm³、3.0kg/Nm³、5.0kg/Nm³、8.0kg/Nm³、10.0kg/Nm³、13.0kg/Nm³、16.0kg/Nm³、19.5.0kg/Nm³And the like, so that carbon dioxide and carbon are subjected to reduction reaction to generate carbon monoxide, the heat of the reaction layer is absorbed, the temperature of the reaction layer is maintained in a reasonable range, and the quality of coal gas and slag are kept from slagging. Preferably, the ratio of the mass of carbon dioxide to the volume of oxygen in the enriched oxygen is set to 1.0 to 15.0kg/Nm³. Utility model people find that if the ratio of the mass of carbon dioxide to the volume of oxygen in the oxygen enrichment is too large, the temperature of a reaction layer is possibly reduced too much, thereby leading to poor gas quality.

Furthermore, the air inflow of the top gasifying agent inlet and the middle gasifying agent inlet is 30-90% (e.g. 30%, 50%, 70%, 90%, etc.) of the total air inflow of the gasifying agent, wherein the air inflow of the top gasifying agent inlet is 70-90% (e.g. 70%, 80%, 90%, etc.) of the total air inflow of the top gasifying agent inlet and the middle gasifying agent inlet, and the air inflow of the middle gasifying agent inlet is 10-30% (e.g. 10%, 20%, 30%, etc.) of the total air inflow of the top gasifying agent inlet and the middle gasifying agent inlet; the air inflow of the bottom gasification agent air inlet is 10-70% (such as 10%, 30%, 50%, 70% and the like) of the total air inflow of the gasification agent. Therefore, by controlling the air inflow of each air inlet of the gasification furnace within the range, the volatile matter in the upper oxidation layer, which generates tar, can be directly oxidized into coal gas by the oxygen in the gasification agent, thereby avoiding the generation of tar, and simultaneously, the carbon in the lower oxidation layer is oxidized by the oxygen in the gasification agent to generate coal gas.

Further, the temperature of the drying layer is 20 to 200 ℃ (e.g., 20 ℃, 60 ℃, 100 ℃, 140 ℃, 180 ℃, 200 ℃, etc.), the temperature of the carbonization layer is 200 to 600 ℃ (e.g., 200 ℃, 300 ℃, 400 ℃, 500 ℃, 600 ℃, etc.), the temperature of the upper oxidation layer is 600 to 1200 ℃ (e.g., 600 ℃, 800 ℃, 1000 ℃, 1200 ℃, etc.), the temperature of the reduction layer is 600 to 1100 ℃ (e.g., 600 ℃, 700 ℃, 800 ℃, 900 ℃, 1000 ℃, 1100 ℃, etc.), the temperature of the lower oxidation layer is 600 to 1100 ℃ (e.g., 600 ℃, 700 ℃, 800 ℃, 900 ℃, 1000 ℃, 1100 ℃, etc.), and the temperature of the ash layer is 200 to 600 ℃ (e.g., 200 ℃, 300 ℃, 400 ℃, 500 ℃, 600 ℃, etc.). Therefore, by controlling the temperature of each reaction area in the gasification furnace to be in the range, the reaction layer of the oxidation layer can maintain reasonable reaction temperature, the quality of coal gas is ensured, and meanwhile, the reaction temperature of ash is lower than the softening point, and no slagging occurs.

(3) And (3) carrying out gasification reaction on the organic solid waste to obtain combustible gas and ash, and discharging the combustible gas out of the reaction zone furnace body through a gas outlet.

(4) And discharging the ash out of the reaction zone furnace body by using a slag discharging device.

(5) And supplying the combustible gas to a secondary combustion chamber for combustion treatment to obtain high-temperature flue gas.

(6) And supplying the high-temperature flue gas to a waste heat boiler for heat exchange treatment to obtain cooling flue gas and superheated steam.

In the step, high-temperature flue gas sequentially passes through a superheater, an evaporator, an economizer and a steam pocket in a hearth; the water absorbs heat in the economizer, the temperature rises to a saturation temperature slightly lower than the pressure of the steam pocket, the water enters the steam pocket, the water entering the steam pocket is mixed with saturated water in the steam pocket and then enters the evaporator along the downcomer to start steam generation, the steam-water mixture enters the steam pocket through the riser to perform steam-water separation, the water enters the downcomer in the water space in the steam pocket to continuously absorb heat and generate steam, and the steam enters the superheater from the upper part of the steam pocket to enable the saturated steam to be changed into superheated steam.

(7) And returning the superheated steam to the fixed bed gasification furnace, and supplying the cooled flue gas to the gas preheater to preheat cold gas to obtain preheated gas and flue gas tail gas.

In the step, the cooling flue gas after waste heat recovery of the waste heat boiler goes through a tube pass, the cold gas enters a shell pass in the gas preheater through a gas blower, and after heat exchange is carried out between the flue gas and the cold gas, the preheated gas is conveyed to the gasification furnace along with a pipeline. Further, the preheated gas is selected from at least one of carbon dioxide, air, and oxygen-enriched air.

(8) And returning the preheated gas to the fixed bed gasification furnace, and allowing the flue gas tail gas to enter a tail gas treatment system.

In the step, the cooled flue gas is treated by a gas preheater, the obtained flue gas tail gas enters a tail gas treatment system through a tail gas outlet, and is introduced into a chimney after being subjected to tail gas treatment processes such as filtering, adsorption, acid washing, dust removal and the like, and is discharged after reaching the standard.

It should be noted that if the preheated gas returned from the gas preheater and/or the superheated steam returned from the waste heat boiler cannot meet the requirement of the fixed bed gasification furnace, the preheated gas and/or the superheated steam are additionally supplemented from another way.

The utility model discloses an in the embodiment not specifically introduce tail gas processing system, the reason lies in being applied to the tail gas processing technique that organic solid waste pyrolysis gasification or gasification burned relatively more ripe, and the suitable purification of flue gas treatment capacity is equipped and can directly be used the utility model provides a tail gas processing system, no longer gives unnecessary details here.

According to the organic solid waste gasification incineration method of the embodiment of the utility model, compared with the direct gasification incineration in the prior art, the gasification process and the gas incineration process of the organic solid waste are separated, the generation of tar can be controlled in the gasification process, the environmental hazard caused by the direct combustion of the tar is effectively avoided, and the cost of the subsequent flue gas treatment is reduced; high-temperature flue gas generated by combustion of fuel gas in the secondary combustion chamber is subjected to waste heat recovery in a waste heat boiler, and generated water vapor is returned to the gasification furnace to be used as a gasification agent, so that the preparation cost of hot air and water vapor is reduced; the flue gas that will pass through waste heat boiler preliminary cooling is supplied with to gas heater, and the flue gas of preliminary cooling carries out the heat exchange with the cold gas and makes the cold gas become preheating gas, and preheating gas returns to the gasifier to gasification efficiency and heat comprehensive utilization efficiency have effectively been improved.

In addition, it should be noted that the organic solid waste mentioned in the embodiment of the present invention includes, but is not limited to, urban organic solid waste (domestic waste, municipal sludge, landscaping waste, etc.), agricultural organic solid waste (crop straw, livestock manure, etc.), industrial organic solid waste (organic waste residue, automobile dismantling waste, etc.), organic hazardous waste, medical waste, etc.

The invention will now be described with reference to specific examples, which are intended to be illustrative only and not to be limiting in any way.

Example 1

The fixed bed gasification furnace of the embodiment adopts a single-channel feeding and wet deslagging design, and has the structure shown in figure 1-3, 1-1 feed inlet, 1-2 feed buffer bin upper valve, 1-3 feed buffer bin, 1-4 feed buffer bin lower valve, 1-5 feed buffer bin pressure charging and discharging port, 1-6 furnace top gasification agent air inlet, 1-7 material distribution device, 1-8 upper furnace body, 1-9 lower furnace body, 1-10 gas outlet, 1-11 membrane water cooling wall, 1-12 furnace grate, 1-13 ash tray, 1-14 furnace bottom gasification agent air inlet, 1-15 epitaxial annular cavity and 1-16 gasification agent distribution regulator, 1-17-middle section gasifying agent gas inlet, 1-18-inert gas purging gas inlet, 1-19-slag ring, 1-20-first ash knife, 1-21-grate supporting piece, 1-22-second ash knife and 1-23-slag breaking block.

(1) Feeding of the feedstock

The organic solid waste gasification furnace of the utility model is composed of a feeding device, a gasification device and a slag discharge device. The feeding device is composed of a feeding port 1-1, an upper valve 1-2 of a feeding buffer bin, a feeding buffer bin 1-3, a lower valve 1-4 of the feeding buffer bin, a pressure charging and releasing port 1-5 of the feeding buffer bin and an inert gas purging air inlet 1-18. The feed inlet 1-1 is positioned at the topmost end of the gasification furnace, and a feed buffer bin upper valve 1-2 is arranged between the feed inlet 1-1 and the feed buffer bin 1-3 and is connected with the feed buffer bin upper valve through a flange. A feeding buffer bin lower valve 1-4 is arranged between the feeding buffer bin 1-3 and the upper furnace body 1-8 and is connected with the feeding buffer bin lower valve through a flange, and a feeding buffer bin pressure charging and releasing port 1-5 which is horizontally arranged is arranged on the side edge of the feeding buffer bin 1-3. The material enters the gasification furnace from the feeding port 1-1, a certain pressure exists in the furnace at the moment, the lower valve 1-4 of the feeding buffer bin keeps a closed state, the upper valve 1-2 of the feeding buffer bin is opened to enable the material in the feeding port to enter the feeding buffer bin 1-3, the feeding buffer bin 1-3 is in a normal pressure state, the upper valve 1-2 of the feeding buffer bin is closed after the material is added into the feeding buffer bin 1-3 to realize the sealing of the feeding buffer bin 1-3, the charging is carried out through the charging and pressure relief port 1-5 of the feeding buffer bin at the moment to enable the pressure in the feeding buffer bin 1-3 to be consistent with the pressure in the reaction furnace, the inert gas at the lower part of the lower valve 1-4 of the feeding buffer bin is used for blowing the nitrogen, the water vapor or the carbon dioxide into the gas inlet 1-18, so that the atmosphere at the lower part of the lower valve 1-4 of the feeding buffer bin is the non-combustible gas, and opening a lower valve 1-4 of the feeding buffer bin to enable the materials in the feeding buffer bin 1-3 to enter an upper-section furnace body 1-8 to be gasified under the action of gravity. After materials in the feeding buffer bin 1-3 completely enter the upper furnace body 1-8, the lower valve 1-4 of the feeding buffer bin is closed, pressure relief is carried out through the pressure relief opening 1-5 of the feeding buffer bin, the normal pressure state is achieved, and the upper valve 1-2 of the feeding buffer bin is opened to start a new round of feeding.

(2) Intake air

The furnace body is internally provided with three gasification agent air inlets, namely a furnace top gasification agent air inlet 1-6, the top of the upper furnace body 1-8 below the inert gas purging air inlet 1-18 is communicated with the upper furnace body 1-8, a plurality of gasification agent air inlets are symmetrically arranged along the circumferential direction, and the top is uniformly distributed with air through symmetrical arrangement. Secondly, the middle section gasification agent gas inlets 1-17 are positioned at the middle section positions of the upper section furnace bodies 1-8, are horizontally arranged along the circumferential direction and are communicated with the upper section furnace bodies 1-8. Thirdly, a bottom gasification agent air inlet 1-14 is communicated with a bottom grate 1-12, bottom uniform air distribution is realized through an air distribution port of the grate 12, and a gasification agent distribution regulator 1-16 is arranged in the grate 1-12. The uniform air distribution of the circumferential air inlets 1-6 and the fire grates 1-12 uniformly distributed on the side edge of the top of the upper furnace body 1-8 can ensure that materials form a uniform and stable reaction layer in the gasification reaction zone, and the phenomenon of uneven reaction is avoided. The middle section gasifying agent air inlets 1-17 are used for controlling the position of the upper oxidation layer, so that the problem that the upper oxidation layer is too high or too low is avoided, when the gasification raw material is low in calorific value or the content of fixed carbon is low, the quantity of gasifying agent fed in the furnace bottom gasifying agent air inlets 1-14 is less, and the small-flow uniform gas distribution is realized by reducing and adjusting the heights of the gasifying agent distribution adjusters 1-16. The gasification agents introduced into the three gasification agent air inlets are air and water vapor.

(3) Gasification process

The gasification reaction area of the organic solid waste gasification furnace of the utility model is mainly positioned in the upper furnace body 1-8 and the lower furnace body 1-9, and the top-down can be divided into a drying layer, a dry distillation layer, an upper oxidation layer, a reduction layer, a lower oxidation layer and a clinker layer. The drying layer, the dry distillation layer and the upper oxidation layer are positioned in the upper section furnace body 1-8, the lower oxidation layer and the ash layer are positioned in the lower section furnace body 1-9, and the reduction layer is positioned at the junction of the upper section furnace body 1-8 and the lower section furnace body 1-9. The material enters the upper furnace body 1-8 from the feeding buffer bin 1-3, the material is uniformly distributed on the drying layer by the distributing device 1-7, the temperature of the drying layer is within the range of 20-200 ℃, moisture in the material is heated and evaporated to enter a gas phase, the dried material enters the dry distillation layer to release volatile matters, tar and coke are generated, and the temperature of the dry distillation layer is within the range of 200-600 ℃. The tar and the coke enter the upper oxidation layer, the tar and the coke are subjected to oxidation reaction with oxygen in a gasifying agent to release heat, so that the temperature of the upper oxidation layer can reach 600-1200 ℃, meanwhile, part of the tar is cracked in a high-temperature region, the coke is only partially subjected to oxidation reaction due to insufficient gas-solid contact, the coke enters the reduction layer under the action of gravity of a material mainly comprising the coke, and carbon dioxide and water generated by oxidation of the upper oxidation layer and the coke of the reduction layer are subjected to gasification reaction, so that the quality of produced gas is improved. The coke which is not reacted in the reduction layer enters the lower oxidation layer and is further oxidized by the gasification agent introduced into the gas inlets 1-14 of the gasification agent at the bottom of the furnace to release heat. The heat of the reduction layer comes from the heat radiation of the upper oxidation layer and the lower oxidation layer, the temperature range is 600-1100 ℃, and the temperature range of the lower oxidation layer is 600-1100 ℃. After the coke is subjected to complete oxidation reaction on the lower oxidation layer, the coke is changed into ash and enters an ash layer above the grate 1-12, and the temperature of the ash layer is within 200-600 ℃. The gasification agent introduced into the air inlet of the furnace bottom gasification agent enters the ash layer through the grate air supply hole to exchange heat with the ash so as to realize the heating of the gasification agent and the cooling of the ash.

(4) Slag discharge

The fire grate 1-12 and the ash tray 1-13 can be driven by a motor to rotate, the ash tray 1-13 and the slag ring 1-19 jointly form an ash tray water seal, water in the ash tray 1-13 is extruded to a certain height to realize a liquid seal under pressure due to certain pressure in the furnace, and gas can burst out of the water when the pressure in the furnace is too high, so that the pressure is safely released, and the potential safety hazard of explosion caused by too high pressure in the furnace is avoided. The big ash knife is welded on the furnace body and the slag ring, the lower end of the big ash knife is inserted into the water of the ash tray, the ash slag is crushed and discharged through the rotation of the grate 1-12 and the ash tray 1-13 and the slag ring and the ash knife, and the ash slag is discharged and collected through a channel corresponding to the ash knife.

(5) Air outlet

The outer layers of the upper furnace body 1-8 and the lower furnace body 1-9 are membrane water-cooling walls 1-11, the membrane water-cooling walls 1-11 are used for preventing the furnace body from generating high-temperature outward radiation heat, and simultaneously effectively preventing the furnace wall from slagging phenomenon caused by high temperature, and simultaneously, compared with the traditional mode of adopting a water jacket, the bulging problem can be effectively avoided. The top of the lower furnace body 1-9 exceeds the top of the upper furnace body 1-8 area and is provided with an epitaxial annular cavity 1-15 communicated with the lower furnace body 1-9, the outside of the epitaxial annular cavity 1-15 is made of refractory brick materials, a gas outlet 1-10 is positioned at the top of the epitaxial annular cavity 1-15 and is horizontally arranged, and the epitaxial annular cavity 1-15 can effectively realize uniform gas outlet, and simultaneously can realize the sedimentation of particles in the gas and reduce the particles in the gas. The gas outlet 1-10 of the coal gas is correspondingly the outlet of the reduction layer, and the sleeve structure is not arranged in the high-temperature area, so that the problem of slag bonding of the sleeve is avoided. Finally, the combustible gas with low tar, low particulate matter and high calorific value is obtained from 1-10 gas outlets.

The following concrete examples of the operation of the gasification furnace are as follows:

the inner diameter of the furnace bottom of the gasification furnace is 3.6m, the treated materials are domestic garbage, and the treatment capacity is 4100 kg/h. The main operating conditions and gasification results were as follows:

(1) the material industry analyses are shown in the following table:

(2) the operating conditions are as follows:

gasification pressure: 7 kPa;

gasifying agent: air + water vapor;

air quantity: 4600Nm³/h；

Amount of water vapor: 500 kg/h.

(3) And (3) gasification result:

gas production: 7200Nm³/h；

The fuel gas comprises the following components: h₂：16.17％，CO：24.80％，CH₄：1.50％，CO₂：6.89％，N₂：50.44％，O₂：0.10％，C_nH_m：0.10％；

Gasification efficiency: 69%;

carbon content of ash: 2.8 percent;

the tar content of the fuel gas is as follows:<1g/Nm³。

example 2

The fixed bed gasification furnace of the embodiment adopts a single-channel feeding and central deslagging design, and has the structure shown in figure 4, 2-1-feeding port, 2-2-feeding buffer bin upper valve, 2-3-feeding buffer bin, 2-4-feeding buffer bin lower valve, 2-5-feeding buffer bin charging and pressure relief port, 2-6-furnace top gasification agent air inlet, 2-7-material distribution device, 2-8-upper furnace body, 2-9-lower furnace body, 2-10-middle gasification agent air inlet, 2-11-coal gas air outlet, 2-12-membrane water cooling wall, 2-13-extension annular cavity, 2-14-grate, 2-15-furnace bottom gasification agent air inlet and 2-16-gasification agent distribution regulator, 2-17-inert gas purging gas inlet, 2-18-slag bin upper valve, 2-19-slag bin, 2-20-slag bin lower valve, 2-21-slag bin pressure charging and releasing port and 2-22-scraper.

(1) Feeding of the feedstock

The basic procedure is as in example 1.

(2) Gasification agent inlet gas

The basic procedure is as in example 1.

(3) Gasification process

The gasification reaction area of the organic solid waste gasification furnace of the embodiment is mainly positioned in the upper section furnace body 2-8 and the lower section furnace body 2-9 and can be divided into a drying layer, a dry distillation layer, an upper oxidation layer, a reduction layer, a lower oxidation layer and an ash residue layer from top to bottom. The drying layer, the dry distillation layer and the upper oxidation layer are positioned in the upper section of furnace body, the lower oxidation layer and the ash layer are positioned in the lower section of furnace body, and the reduction layer is positioned at the junction of the upper section of furnace body 2-8 and the lower section of furnace body 2-9. The material enters an upper-section furnace body 2-8 from a feeding buffer bin 2-3, the material is uniformly distributed on a drying layer by a distributing device 2-7, the temperature of the drying layer is within the range of 20-200 ℃, moisture in the material is heated and evaporated to enter a gas phase, the dried material enters a dry distillation layer to release volatile matters, tar and coke are generated, and the temperature of the dry distillation layer is within the range of 200-600 ℃. The tar and the coke enter the upper oxidation layer, the tar and the coke are subjected to oxidation reaction with oxygen in a gasifying agent to release heat, so that the temperature of the upper oxidation layer can reach 600-1200 ℃, meanwhile, part of the tar is cracked in a high-temperature region, the coke is only partially subjected to oxidation reaction due to insufficient gas-solid contact, the coke enters the reduction layer under the action of gravity of a material mainly comprising the coke, and carbon dioxide and water generated by oxidation of the upper oxidation layer and the coke of the reduction layer are subjected to gasification reaction, so that the quality of produced gas is improved. The coke which is not reacted in the reduction layer enters the lower oxidation layer and is further oxidized by the gasification agent introduced into the gas inlet 2-15 of the gasification agent at the bottom of the furnace to release heat. The heat of the reduction layer comes from the heat radiation of the upper oxidation layer and the lower oxidation layer, the temperature range is 600-1100 ℃, and the temperature range of the lower oxidation layer is 600-1100 ℃. The coke is completely oxidized in the lower oxidation layer and then is changed into ash to enter an ash layer above the grate 2-14, the temperature range of the ash layer is 200-600 ℃, the grate 2-14 is driven to rotate by a motor, the slag in the upper ash layer is broken by the scrapers 2-22, the blockage of large slag is avoided, and the slag enters the slag bin 2-19 through a collecting port below the grate 2-14. The gasification agent introduced into the furnace bottom gasification agent inlet 2-15 enters the ash layer through the grate 2-14 air distribution holes to exchange heat with the ash so as to realize the heating of the gasification agent and the cooling of the ash.

(4) Slag discharge

The slag bin 2-19 is alternately discharged with ash, the lower valve 2-20 is closed, the upper valve 2-18 is opened, the ash is crushed by the grate 2-14 and enters the slag bin 2-19 along the central collecting port below under the action of gravity, then the upper valve 2-18 is closed, the pressure of the slag bin is changed into normal pressure by the pressure relief through the pressure relief opening 2-21, the lower valve 2-20 is opened to discharge the ash, then the lower valve 2-20 is closed, the pressure is charged through the pressure relief opening 2-21, the pressure of the slag bin is the same as that in the furnace, and then the upper valve 2-18 is opened to enable the ash in the ash layer to enter the slag bin to start a new round of slag discharge.

(5) Air outlet

The basic procedure is as in example 1.

Example 3

The fixed bed gasification furnace of the embodiment adopts a double-channel feeding and side deslagging design, and the structure of the fixed bed gasification furnace is shown in figure 5, wherein 3-1a and 3-1b are respectively a feeding buffer bin upper valve, 3-2a and 3-2b are respectively a feeding buffer bin charging and pressure relief opening, 3-3a and 3-3b are respectively a feeding buffer bin, 3-4a and 3-4b are respectively a feeding buffer bin lower valve, 3-5a and 3-5b are respectively an inert gas purging air inlet, 3-6 feed inlets, 3-7 transition bins, 3-8 furnace top gasification agent air inlets, 3-9 distribution devices, 3-10 upper furnace bodies, 3-11 lower furnace bodies, 3-12 coal gas outlets and 3-13 membrane type water cooling walls, 3-14-epitaxial annular cavity, 3-15-middle section gasifying agent inlet, 3-16-grate, 3-17-bottom gasifying agent inlet, 3-18-gasifying agent distribution regulator, 3-19-upper slag bin valve, 3-20-slag bin, 3-21-lower slag bin valve, 3-22-slag bin charge and discharge and 3-23-feeding buffer bin communicating valve.

(1) Feeding of the feedstock

The fixed bed gasifier of this embodiment adopts the design of binary channels feeding. The double-channel feeding work flow is that when the feeding buffer bin 3-3a is in a normal pressure state, the feeding buffer bin communication valve 3-23 and the feeding buffer bin lower valve 3-4a are in a closed state, the feeding buffer bin upper valve 3-1a is in an open state, materials enter the feeding buffer bin 3-3a through the feeding port 3-6 through the opened feeding buffer bin upper valve 3-1a, then the feeding buffer bin upper valve 3-1a is closed, and the feeding buffer bin 3-3a forms a normal pressure closed space. Meanwhile, the pressure in the feeding buffer bin 3-3b is the same as the pressure in the furnace through a charging pressure relief opening 3-2b of the feeding buffer bin, nitrogen, water vapor or carbon dioxide is introduced through an inert gas purging air inlet 3-5b at the lower part of a lower valve 3-4b of the feeding buffer bin, so that the atmosphere at the lower part of the lower valve 3-4b of the feeding buffer bin is non-combustible gas, the lower valve 3-4b of the feeding buffer bin is opened, the material falls into a transition bin 3-7 under the action of gravity, the gas in the transition bin 3-7 enters the feeding buffer bin 3-3b, then the lower valve 3-4b of the feeding buffer bin is closed, a communicating valve 3-23 of the feeding buffer bin is opened, so that the high-pressure gas in the feeding buffer bin 3-3b enters the feeding buffer bin 3-3a, the pressure of the two feeding buffer bins is the same, at the moment, the connecting valve 3-23 of the feeding buffer bin is closed, the feeding buffer bin 3-3b without materials is decompressed through the charging decompression port 3-2b of the feeding buffer bin, the feeding buffer bin 3-3b is changed into a normal pressure state, then the upper valve 3-1b of the feeding buffer bin is opened for charging, the feeding buffer bin 3-3a with materials is pressurized through the charging decompression port 3-2a of the feeding buffer bin, the pressure is the same as the pressure in the furnace, the gas inlet 3-5a is purged through inert gas at the lower part of the lower valve 3-4a of the feeding buffer bin, nitrogen, water vapor or carbon dioxide is introduced, the atmosphere at the lower part of the lower valve 3-4a of the feeding buffer bin is non-combustible gas, then the lower valve 3-4a of the feeding buffer bin is opened, and the materials enter the transition bin 3-7 under the action of gravity, the two feeding buffer bins work alternately, so that the pressure charging and releasing efficiency can be effectively improved, and the dust-containing gas discharged in the pressure releasing process is reduced.

(2) Gasification agent inlet gas

The reaction zone furnace body mainly comprises a furnace top gasification agent air inlet 3-8, a material distribution device 3-9, an upper section furnace body 3-10, a coal gas air outlet 3-12, a lower section furnace body 3-11, a furnace grate 3-16, a furnace bottom gasification agent air inlet 3-17, a membrane water wall 3-13, a gasification agent distribution regulator 3-18 and a middle section gasification agent air inlet 3-15. The furnace top gasification agent air inlets 3-8 are arranged on the side edges of the transition bins 3-7, a plurality of furnace top gasification agent air inlets 3-8 are symmetrically arranged along the circumferential direction, and a cavity and a plurality of air inlets are formed in the regions of the transition bins 3-7, so that the top part is uniformly distributed. The middle section gasification agent air inlets 3-15 are positioned on the upper part of the middle section of the furnace body and are communicated with the upper section furnace body 3-10 to be horizontally arranged along the circumferential direction for regulating and controlling the position of the upper oxidation layer and avoiding the problem that the upper oxidation layer is too high or too low. The bottom gasification agent air inlet is communicated with the bottom grate 3-16, and the bottom is uniformly distributed through the air distribution holes on the grate 3-16. When the gasification raw material is low in calorific value or the fixed carbon content is low, the gasification agent supply quantity demand of the furnace bottom gasification agent air inlets 3-17 is low, and the small-flow uniform gas distribution is realized by reducing the height of the gasification agent distribution regulator. The uniform air distribution of the furnace top gasification agent air inlets 3-8 and the furnace bottom gasification agent air inlets 3-17 can ensure that materials form a uniform and stable reaction layer in the gasification reaction zone, and the phenomenon of uneven reaction is avoided. The gasifying agents introduced into the two air inlets are air and water vapor. The material distribution device is positioned at the upper part of the gasification furnace body right below the transition bin 3-7, and the materials falling into the furnace from the transition bin 3-7 are uniformly distributed in the furnace through the material distribution device. The outer layer of the furnace body is a membrane type water-cooled wall 3-13, so that the radiation of high temperature in the furnace to the outside is avoided, the slag bonding phenomenon of the inner wall of the furnace is also avoided, and compared with the traditional mode of adopting a water jacket, the bulging problem can be effectively avoided.

(3) Gasification process

The basic procedure is as in example 1.

(4) Slag discharge

The slag bin 3-20 below the furnace body is alternately discharged with ash, the lower valve 3-21 of the slag bin is in a closed state, the upper valve 3-19 of the slag bin is in an open state, ash and slag enter the slag bin through a slag discharge port on the side after being crushed by the grate 3-16, then the upper valve of the slag bin is closed, the pressure is released through the pressure release port of the slag bin, the pressure of the slag bin is changed into a normal pressure state, the lower valve of the slag bin is opened to discharge the ash and slag, then the lower valve of the slag bin is closed, the pressure is released through the pressure release port of the slag bin, the pressure of the slag bin is the same as that in the furnace, and then the upper valve of the slag bin is opened to enable the ash and slag layer to enter the slag bin to discharge a new round.

(5) Air outlet

The basic procedure is as in example 1.

Example 4

A waste heat recovery system was constructed using the fixed-bed gasification furnace set of example 1, and its structure is shown in fig. 6. In fig. 6: 100-fixed bed gasification furnace, 2-second combustion chamber, 21-combustion-supporting blower, 3-waste heat boiler, 31-steam drum, 32-steam release valve, 301-steam pipeline, 4-gas preheater, 41-blower, 42-hot air release valve, 401-hot air pipeline.

The fixed bed gasification furnace of the embodiment 1 is utilized to pressurize and gasify the organic solid waste, the high-temperature combustible gas generated by gasification firstly enters the secondary combustion chamber 2 from the gas outlet through the flue, the high-temperature combustible gas is completely combusted under the action of secondary combustion-supporting air, and the time for high-temperature combustion of the high-temperature combustible gas in the secondary combustion chamber 2 is required to be ensured not to be less than 2 seconds, so that toxic substances such as dioxin and the like in the flue gas are decomposed under the high-temperature condition.

Supplying the high-temperature flue gas to a waste heat boiler for heat exchange treatment, wherein the high-temperature flue gas sequentially passes through a superheater (not shown in the figure), an evaporator (not shown in the figure), an economizer (not shown in the figure) and a steam drum in a hearth; the water absorbs heat in the economizer, the temperature rises to a saturation temperature slightly lower than the pressure of the steam pocket, the water enters the steam pocket, the water entering the steam pocket is mixed with saturated water in the steam pocket and then enters the evaporator along the downcomer to start steam generation, the steam-water mixture enters the steam pocket through the riser to perform steam-water separation, the water enters the downcomer in the water space in the steam pocket to continuously absorb heat and generate steam, and the steam enters the superheater from the upper part of the steam pocket to enable the saturated steam to be changed into superheated steam. The generated superheated steam returns to the hearth of the gasification furnace through a steam pipeline 301; the temperature of the flue gas is reduced to about 310-350 ℃ and then the flue gas enters the gas preheater 4.

The flue gas after the preliminary cooling immediately enters the gas preheater 4 at the tail end of the flue, the air brought into the gas preheater 4 by the air blower 41 is heated through heat exchange, the cooling flue gas after waste heat recovery of the waste heat boiler passes through the tube side, the cold air passes through the shell side, and after the heat exchange is carried out between the hot flue gas and the cold air, the preheated air returns to the fixed bed gasification furnace 100 through the hot air pipeline 401. After the cooling flue gas is treated by a gas preheater, the obtained flue gas tail gas enters a tail gas treatment system through a tail gas outlet, is introduced into a chimney after being subjected to tail gas treatment processes such as filtering, adsorption, acid washing, dust removal and the like, and is discharged after reaching the standard.

In the description herein, references to the description of the term "one embodiment," "some embodiments," "an example," "a specific example," or "some examples," etc., mean that a particular feature, structure, material, or characteristic described in connection with the embodiment or example is included in at least one embodiment or example of the invention. In this specification, the schematic representations of the terms used above are not necessarily intended to refer to the same embodiment or example. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more embodiments or examples. Furthermore, various embodiments or examples and features of different embodiments or examples described in this specification can be combined and combined by one skilled in the art without contradiction.

Although embodiments of the present invention have been shown and described, it is understood that the above embodiments are exemplary and should not be construed as limiting the present invention, and that variations, modifications, substitutions and alterations can be made to the above embodiments by those of ordinary skill in the art without departing from the scope of the present invention.

Claims (10)

1. The organic solid waste gasification incineration system is characterized by comprising: the system comprises a fixed bed gasification furnace, a secondary combustion chamber, a waste heat boiler and a gas preheater;

the fixed bed gasification furnace comprises a feeding device, a reaction zone furnace body, a furnace top gasifying agent air inlet, a middle section gasifying agent air inlet, a furnace bottom gasifying agent air inlet, a coal gas air outlet and a slag discharging device;

the reaction zone furnace body is arranged below the feeding device and comprises an upper section furnace body and a lower section furnace body, the outer diameter of the upper section furnace body is smaller than the inner diameter of the lower section furnace body, the upper section furnace body is partially sleeved in the lower section furnace body, an epitaxial annular cavity is formed by the overlapped part of the upper section furnace body and the lower section furnace body, and a sealing element is arranged at the top of the epitaxial annular cavity; a grate is arranged at the bottom in the lower section furnace body;

the furnace top gasification agent gas inlet is arranged on the top and/or the upper part of the upper-section furnace body and extends into the upper-section furnace body;

the middle-section gasifying agent air inlet is arranged below the furnace top gasifying agent air inlet, is arranged on the side wall of the upper-section furnace body and extends into the upper-section furnace body;

the furnace bottom gasification agent air inlet is communicated with the lower part of the grate;

the gas outlet is arranged on the side wall of the lower furnace body corresponding to the epitaxial annular cavity and is communicated with the epitaxial annular cavity;

the slag discharging device is arranged below or laterally below the lower furnace body;

the secondary combustion chamber is provided with a coal gas inlet and a high-temperature flue gas outlet, and the coal gas inlet is connected with the coal gas outlet;

the waste heat boiler is provided with a high-temperature flue gas inlet, a superheated steam outlet and a cooling flue gas outlet, the high-temperature flue gas inlet is connected with the high-temperature flue gas outlet, and the superheated steam outlet is connected with the air inlet of the fixed bed gasification furnace;

the gas preheater is provided with a cooling flue gas inlet, a cold gas inlet, a preheating gas outlet and a tail gas outlet, wherein the cooling flue gas inlet is connected with the cooling flue gas outlet, and the preheating gas outlet is connected with the gas inlet of the fixed bed gasification furnace.

2. The organic solid waste gasification incineration system of claim 1, wherein the feeding device comprises at least one feeding channel, each feeding channel is provided with a feeding hole, an upper feeding buffer bin valve, a feeding buffer bin, a lower feeding buffer bin valve and an inert gas purging air inlet from top to bottom in sequence, and a feeding buffer bin pressure charging and discharging port is formed in the side of the feeding buffer bin;

the top of the upper-section furnace body is connected with the feeding device through a transition bin, the transition bin is communicated with a furnace chamber of the reaction zone furnace body, and a furnace top gasification agent air inlet is arranged on the side wall of the transition bin;

the feeding device comprises two feeding channels, and a communicating valve is arranged between feeding buffer bins of the two feeding channels; and the discharge end of the feeding channel is communicated with the transition bin and is positioned above the furnace top gasifying agent air inlet.

3. The organic solid waste gasification incineration system of claim 1, wherein the slag discharge device has a structure of one of:

(1) the slag discharging device sequentially comprises an upper slag bin valve, a slag bin and a lower slag bin valve from top to bottom, and a slag bin pressure charging and releasing port is arranged on the side part of the slag bin;

the lower part of the lower furnace body is in an inverted cone shape, the bottom of the lower furnace body is provided with a slag outlet, and the slag discharging device is arranged below the lower furnace body and is connected with the slag outlet;

the side wall of the lower part of the lower furnace body is provided with a slag outlet, and the slag discharging device is arranged below the side of the lower furnace body and is connected with the slag outlet;

the fire grate is rotatably arranged, and a cloth air port is formed on the fire grate;

(2) or the slag discharging device is arranged in water and is positioned below the reaction zone furnace body, the slag discharging device comprises an ash tray, a slag crushing ring, a grate supporting piece and a first ash knife, the ash tray is arranged below the grate, the slag crushing ring is annular and is sleeved in the ash tray, the grate supporting piece is arranged below the grate and is positioned in the slag crushing ring, and the first ash knife is arranged on the inner side wall of the ash tray;

the slag discharging device also comprises a second ash knife and a slag breaking block, the second ash knife is arranged at the bottom of the grate supporting piece, and the slag breaking block is arranged on the side wall of the grate supporting piece;

the fire grate is rotatable, a cloth air port is formed on the fire grate, and the fire grate supporting piece is used for supporting the fire grate and rotates along with the fire grate.

4. The organic solid waste gasification incineration system of claim 1, further comprising a gasification agent distribution regulator, wherein the gasification agent distribution regulator is movably disposed at an outlet end of the bottom gasification agent inlet port up and down, and is located inside the grate.

5. The organic solid waste gasification incineration system of claim 1, further comprising a distribution device disposed above the inside of the upper stage furnace body.

6. The organic solid waste gasification incineration system of claim 1, wherein a plurality of top gasification agent inlets are provided, and the plurality of top gasification agent inlets are symmetrically arranged along the circumferential direction of the reaction zone furnace body;

the middle-section gasification agent gas inlets are arranged symmetrically along the circumferential direction of the reaction zone furnace body.

7. The organic solid waste gasification incineration system of any one of claims 1 to 6, wherein the height of the epitaxial annular cavity is 10% to 30% of the total height of the reaction zone furnace body;

the ratio of the width of the epitaxial annular cavity to the inner diameter of the furnace body of the reaction zone is (0.1-0.3): 1.

8. The organic solid waste gasification incineration system of any one of claims 1 to 6, wherein the inner diameter of the upper section furnace body is 0.3 to 8.0m, and the inner diameter of the lower section furnace body is 0.4 to 8.0 m;

the height of the upper furnace body is 40-80% of the total height of the reaction zone furnace body;

the height between the upper-section furnace body and the fire grate is 20-60% of the total height of the reaction zone furnace body.

9. The organic solid waste gasification incineration system according to any one of claims 1 to 6, wherein the secondary combustion chamber is further provided with an induced draft fan inlet arranged at the lower part of the coal gas inlet, and the induced draft fan is used for supplementing a combustion improver into the secondary combustion chamber;

the gas preheater is of a box type tubular structure, the cooling flue gas passes through a tube pass, and the cold air passes through a shell pass;

and an air escape valve is arranged above the gas preheater.

10. The organic solid waste gasification incineration system of any one of claims 1 to 6, wherein the outside of the upper furnace body and the lower furnace body is a membrane water wall or a jacket water wall;

the membrane water-cooling wall is a tube type membrane water-cooling wall or a coil type membrane water-cooling wall.

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