Gasification process method for coupling fluidized bed with moving filter bed

Abstract

The invention belongs to the field of fluidized bed gasification processes, and particularly discloses a gasification process method for coupling a fluidized bed with a moving filter bed, which comprises the following steps: S1, adding a carbon-containing raw material into the moving filter bed; s2, the fluidized bed gasification furnace generates high-temperature crude synthesis gas; s3, introducing the high-temperature crude synthesis gas into a moving filter bed; s4, the moving filter bed adsorbs and filters fly ash in the high-temperature crude synthesis gas through a carbon-containing raw material, and purified synthesis gas is generated; s5, moving the carbon-containing raw material in the filter bed to generate pyrolysis gas and a carbonized material; s6, leading out the purified synthesis gas and the pyrolysis gas from the moving filter bed; and S7, leading out the carbonized material from the moving filter bed or returning the carbonized material to the fluidized bed gasifier. Through the coupling design of the fluidized bed and the moving filter bed, the carbon-containing raw material of the moving bed is driven to be pyrolyzed by using the waste heat of the synthesis gas, and the dust removal of the synthesis gas, the adsorption of harmful impurities and the pyrolysis recycling of the carbon-containing raw material are synchronously realized in a'one-bed dual-purpose 'mode; carbon resources in the fly ash can also be returned to the furnace for re-gasification, so that the effective gas yield is further improved.

Description

Technical Field

[0001] The present invention belongs to the field of fluidized bed gasification technology, and in particular relates to a gasification technology method of a fluidized bed coupled with a moving filter bed. Background Art

[0002] Fluidized bed gasification technology is widely used in coal chemical industry, biomass energy, and solid waste treatment due to its wide adaptability to feedstocks and high gasification intensity. However, this process has inherent drawbacks: the crude syngas carries a large amount of high-carbon fly ash. Due to the high material circulation rate within the fluidized bed, conventional cyclone separators are inefficient in capturing fine fly ash, causing the fly ash to enter subsequent systems along with the syngas.

[0003] Since the synthesis gas carries a high concentration of fly ash, the subsequent equipment failure rate increases, such as wear, blockage, corrosion of the heat exchanger, and failure of the filter, which affects the long-term stable operation of the system.

[0004] In fluidized bed gasification projects for low-ash melting point raw materials such as biomass / solid waste treatment, the high-temperature synthesis gas exiting the gasifier after dust removal by a cyclone dust collector contains a large amount of dust, biomass tar, methane and other components, which cannot meet the demand for synthetic methanol and other related chemical products.

[0005] The subsequent processing route, due to the difficulty in selecting economical and reliable high-temperature filtration equipment to meet process requirements, requires cooling the synthesis gas first and then removing dust. Once the requirements are met, the tar and methane are then subjected to high-temperature pyrolysis in a POX furnace. This process requires the addition of high-dust-resistant heat exchange and filtration equipment, which consumes a large amount of energy and reduces the economic efficiency and stability of the system.

[0006] If the synthesis gas is directly fed into the POX furnace, the high-dust synthesis gas will produce a slag reaction in the POX furnace, resulting in complex design of the POX furnace and supporting waste heat recovery systems, increased equipment investment, and reduced operational reliability.

[0007] To address this issue, traditional processes are forced to add a variety of additional treatment processes: such as adding fly ash secondary return to the furnace for regasification, increasing the filtration capacity of the filter, adding water washing and dust removal facilities, etc.; this will significantly increase the investment scale and operating costs of the device, making the stability and economy of the system operation worse. Summary of the Invention

[0008] The purpose of the present invention is to provide a gasification process method of a fluidized bed coupled with a moving filter bed to solve the problems proposed in the above background technology that the traditional gasification process requires the addition of multiple processing processes, has high investment scale and operating costs, and has poor stability and economy.

[0009] To achieve the above object, the present invention provides the following technical solutions:

[0010] A gasification process method of a fluidized bed coupled with a moving filter bed, comprising:

[0011] S1, adding carbon-containing raw materials to the mobile filter bed through the feeding device;

[0012] S2. introducing a gasifying agent into the fluidized bed gasifier to generate a high-temperature crude synthesis gas containing fly ash;

[0013] S3, passing the high-temperature crude synthesis gas into a moving filter bed;

[0014] S4, the mobile filter bed absorbs and filters fly ash, alkali metals, and chlorine in the high-temperature raw synthesis gas through the carbon-containing raw material to generate purified synthesis gas;

[0015] S5. The carbon-containing raw materials in the mobile filter bed are heated to 700-1000°C by the high-temperature crude synthesis gas in an oxygen-free environment, undergoing drying, pyrolysis and hydrocracking to generate pyrolysis gas and carbonized material;

[0016] S6, the purified synthesis gas and pyrolysis gas are led out through the moving filter bed;

[0017] S7. The carbonized material is drawn out from the mobile filter bed as raw material for activated carbon production, or returned to the fluidized bed gasifier as gasification raw material.

[0018] Preferably, in step S3, before the high-temperature crude synthesis gas is passed into the mobile filter bed, the high-temperature crude synthesis gas is pre-dusted by a cyclone dust collector.

[0019] Preferably, the feeding device includes a silo, a lock hopper and a sending hopper. The output end of the silo is connected to the lock hopper input end through a lock hopper feed valve, the output end of the lock hopper is connected to the sending hopper input end through a sending hopper feed valve, the output end of the sending hopper is connected to the top feed port of the mobile filter bed through a sending hopper discharge valve, and a variable frequency feeder is arranged between the sending hopper discharge valve and the mobile filter bed.

[0020] Preferably, a carbonized material discharge port is provided at the bottom of the movable filter bed, and a movable bed discharge device is provided between the carbonized material discharge port and the fluidized bed gasifier for drawing out the carbonized material and sending it to the fluidized bed gasifier.

[0021] Preferably, the lock hopper is provided with a lock hopper pressure charging valve, the sending hopper is provided with a sending hopper pressure stabilizing valve, the moving filter bed is provided with a feed inlet protection gas valve, and the moving bed discharge device is provided with a moving bed return material conveying gas control valve, all of which are used to control the introduction of protective gas.

[0022] Preferably, a carbonized material outlet is provided at the bottom of the mobile filter bed.

[0023] Preferably, a dust collector discharging device is provided between the cyclone dust collector and the fluidized bed gasifier, for sending the fly ash captured by the cyclone dust collector to the bottom of the fluidized bed gasifier for further gasification.

[0024] Preferably, the gasifying agent includes superheated steam and oxygen / air, and the fluidized bed gasifier is respectively provided with a distribution plate air intake control valve and two central tube air intake control valves. The distribution plate air intake control valve is used to control the gasifying agent to pass into the fluidized bed gasifier through the small holes of the distribution plate, and the central tube air intake control valve is used to control the gasifying agent to pass into the fluidized bed gasifier through the central tube.

[0025] Preferably, a slag discharge buffer hopper is provided at the bottom of the fluidized bed gasification furnace for temporarily storing bottom slag discharged from the fluidized bed gasification furnace.

[0026] Preferably, a gas distributor is provided in the moving filter bed for distributing the high-temperature raw synthesis gas introduced into the moving filter bed.

[0027] Compared with the prior art, the present invention has the following beneficial effects:

[0028] The present invention uses a coupling design of a fluidized bed and a mobile filter bed to simultaneously achieve synthesis gas dust removal, harmful impurity adsorption and carbon-containing raw material pyrolysis resource utilization in a "one bed, two purposes" manner, completely omitting traditional filters (bags or metal / ceramic filter elements, etc.), reducing equipment investment; utilizing the waste heat of synthesis gas to drive the pyrolysis of the moving bed, the carbon resources in the fly ash are returned to the furnace for re-gasification and utilization, and the effective gas yield is improved; at the same time, harmful substances such as alkali metals / chlorine are adsorbed, extending the continuous operation cycle of the system, and providing a highly economical, low-emission integrated solution for coal chemical industry, biomass and solid waste gasification.

[0029] The present invention can reduce the temperature of the synthesis gas by continuously adding cold materials into the mobile filter bed and continuously exchanging heat with the high-temperature coal gas produced by the gasifier. This not only improves the waste heat utilization efficiency of the system, but also allows the high-temperature materials to return to the furnace and directly enter the gasifier instead of the cold materials, thereby reducing the oxygen consumption of the gasifier and increasing the effective gas content (CO+H2+CH4) of the synthesis gas components, thereby improving the economic benefits of the gasifier operation. BRIEF DESCRIPTION OF THE DRAWINGS

[0030] In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the following briefly introduces the drawings required for describing the embodiments. Obviously, the drawings described below are only some embodiments of the present invention. Those skilled in the art can also derive other drawings based on these drawings without inventive effort. Among them:

[0031] Figure 1 A flowchart of the method steps of the present invention;

[0032] Figure 2 It is a schematic diagram of the process flow of the present invention.

[0033] In the figure: W1, carbon-containing raw material; W2, protective gas; W3, purified synthesis gas; W4, superheated steam; W5, oxygen / air; V1, silo; V2, lock hopper; V3, sending hopper; V4, moving filter bed; V5, fluidized bed gasifier; V6, cyclone dust collector; V7, moving bed discharge device; V8, dust collector discharge device; V9, slag buffer hopper; F1, lock hopper pressure charging valve; F2, lock hopper feed valve; F3, sending hopper pressure stabilizing valve; F4, sending hopper feed valve; F5, feed port protective gas valve; F6, sending hopper discharge valve; F7, moving bed return material conveying gas control valve; F8, distribution plate air inlet control valve; F9, center pipe superheated steam inlet control valve; F10, center pipe oxygen / air inlet control valve; G, variable frequency feeder; N1, carbonized material outlet; N2, carbonized material outlet. DETAILED DESCRIPTION

[0034] In order to make the above-mentioned objects, features and advantages of the present invention more obvious and easy to understand, the specific embodiments of the present invention are described in detail below with reference to the accompanying drawings.

[0035] In the following description, many specific details are set forth to facilitate a full understanding of the present invention. However, the present invention may also be implemented in other ways different from those described herein. Those skilled in the art may make similar generalizations without violating the connotation of the present invention. Therefore, the present invention is not limited to the specific embodiments disclosed below.

[0036] Secondly, the term "one embodiment" or "embodiment" herein refers to a specific feature, structure, or characteristic that may be included in at least one implementation of the present invention. The phrase "in one embodiment" appearing in various places throughout this specification does not necessarily refer to the same embodiment, nor does it refer to a separate or selective embodiment that is mutually exclusive of other embodiments.

[0037] As attached Figure 1 and attached Figure 2 As shown:

[0038] Example 1: This example provides a gasification process method of a fluidized bed coupled with a moving filter bed, comprising:

[0039] S1, adding carbonaceous raw material W1 to the moving filter bed V4 through the feeding device;

[0040] S2, introducing a gasifying agent into the fluidized bed gasifier V5 to generate a high-temperature raw synthesis gas containing fly ash;

[0041] S3, introducing high-temperature crude synthesis gas from the lower middle part of the moving filter bed V4;

[0042] S4, the mobile filter bed V4 absorbs and filters the fly ash, alkali metals and chlorine in the high-temperature raw synthesis gas through the carbon-containing raw material W1 to generate the purified synthesis gas W3;

[0043] S5, the carbonaceous raw material W1 in the mobile filter bed V4 is heated to 700-1000°C by the high-temperature crude synthesis gas in an oxygen-free environment, undergoing drying, pyrolysis and hydrocracking to generate pyrolysis gas and carbonized material;

[0044] S6, the purified synthesis gas W3 and the pyrolysis gas are drawn out from the upper middle part of the moving filter bed V4;

[0045] S7. The carbonized material is drawn out from the bottom of the moving filter bed V4 and returned to the fluidized bed gasifier V5 as a gasification raw material.

[0046] The fluidized bed gasifier V5 is also equipped with a direct feeding mechanism for separately feeding the fluidized bed gasifier V5 with charge materials. The charge materials include coal, biomass, industrial carbon-containing waste, and domestic garbage. After the gasifying agent is introduced, a gasification reaction occurs in the fluidized bed gasifier V5, generating high-temperature crude synthesis gas containing fly ash. The gas carries small dust particles upward, is discharged through the top outlet of the fluidized bed gasifier V5, and is introduced into the mobile filter bed V4.

[0047] At this time, the feeding device will add the carbon-containing raw material W1 into the mobile filter bed V4 from the top inlet and move it downward, while the high-temperature crude synthesis gas moves upward, and a two-way interactive reaction occurs. At the same time, the dust in the high-temperature crude synthesis gas is filtered and adsorbed by the solid carbon-containing raw material W1, and the high temperature of the high-temperature crude synthesis gas is used to dry, dehydrate, devolatilize and thermally crack the carbon-containing raw material W1 to form high-temperature carbonized material and pyrolysis gas. The high-temperature carbonized material is drawn out from the bottom of the mobile filter bed V4 and returned to the fluidized bed gasifier V5 as a furnace feed. Since part of the heat energy in the high-temperature crude synthesis gas is transferred to the carbonized material, the high-temperature carbonized material replaces part of the cold feed of the fluidized bed gasifier V5 when returning to the bottom of the fluidized bed gasifier V5, thereby reducing the total oxygen intake of the fluidized bed gasifier V5 and increasing the effective gas content (CO+H2+CH4), thereby ultimately reducing the production cost of the fluidized bed.

[0048] Purified synthesis gas W3 and pyrolysis gas are drawn out from the upper middle portion of the mobile filter bed V4 and sent to downstream processing stages. For example, if coal is used as a furnace charge and carbonaceous raw material W1 is used to produce synthesis gas, the synthesis gas can be directly introduced into a high-temperature waste heat boiler to recover heat energy, and then washed with water for cooling, dust removal, and ammonia removal. Because the raw coal is directly dried, distilled, and thermally cracked in an oxygen-free, high-temperature, high-hydrogen, and high-water environment, the gas is rich in methane. The methane content in the crude synthesis gas can reach over 15% (the methane content is related to the type of coal), making it very suitable for coal-to-natural gas projects.

[0049] For example, if biomass is gasified to synthesize green alcohol, green ammonia, green jet fuel, etc., the gas can be directly introduced into a high-temperature converter (POX furnace) to carry out high-temperature conversion of methane, tar and other components therein, and then the heat is recovered through a waste heat boiler. After entering a water washing unit, it can be sent to a conversion and synthesis unit as synthesis gas.

[0050] Example 2: This example is basically the same as the previous example, except that, in step S3, before the high-temperature crude synthesis gas is introduced from the lower middle portion of the mobile filter bed V4, the high-temperature crude synthesis gas is pre-dusted by the cyclone dust collector V6.

[0051] The high-temperature crude synthesis gas enters the cyclone dust collector V6 through the top outlet of the fluidized bed gasifier V5. The cyclone dust collector V6 intercepts and filters the fly ash in the high-temperature crude synthesis gas. After dust removal, the high-temperature crude synthesis gas is introduced into the mobile filter bed V4 after leaving the cyclone dust collector V6.

[0052] Example 3: This example is basically the same as the previous example, except that the feeding device includes a silo V1, a lock hopper V2 and a sending hopper V3. The output end of the silo V1 is connected to the input end of the lock hopper V2 through the lock hopper feed valve F2, the output end of the lock hopper V2 is connected to the input end of the sending hopper V3 through the sending hopper feed valve F4, the output end of the sending hopper V3 is connected to the top feed port of the mobile filter bed V4 through the sending hopper discharge valve F6, and a variable frequency feeder G is arranged between the discharge valve of the sending hopper V3 and the mobile filter bed V4.

[0053] Specifically, a carbonized material discharge port N2 is provided at the bottom of the mobile filter bed V4, and a mobile bed discharge device V7 is provided between the carbonized material discharge port N2 and the fluidized bed gasifier V5 for drawing out the carbonized material and sending it to the fluidized bed gasifier V5.

[0054] Specifically, the lock hopper V2 is provided with a lock hopper pressure charging valve F1, the sending hopper V3 is provided with a sending hopper pressure stabilizing valve F3, the mobile filter bed V4 is provided with a feed inlet protection gas valve F5, and the mobile bed discharge device V7 is provided with a mobile bed return material conveying gas control valve F7, all of which are used to control the entry of protective gas W2.

[0055] The carbon-containing raw material W1 is pre-stored in the silo V1 and enters the lock hopper V2 through the lock hopper feed valve F2 by gravity. The amount of protective gas W2 introduced is then controlled by the lock hopper pressure valve F1, so that the pressure in the lock hopper V2 is slightly higher than that in the sending hopper V3. At this time, the sending hopper feed valve F4 is opened to add the carbon-containing raw material W1 into the sending hopper V3 under pressure. Through the above operation, the sending hopper pressure-stabilizing valve F3 is used to control the pressure in the sending hopper V3 to be slightly higher than that in the moving filter bed V4. After opening the sending hopper discharge valve F6, the frequency of the variable frequency feeder G is controlled to automatically and continuously add the carbon-containing raw material W1 to the moving filter bed V4.

[0056] The high-temperature carbonized material after the reaction is discharged to the moving bed discharge device V7 through the carbonized material discharge port N2, and the protective gas W2 is introduced through the moving bed return gas control valve F7. The high-temperature carbonized material is pneumatically conveyed to the fluidized bed gasifier V5 for further gasification;

[0057] The protective gas W2 is not only used for pneumatic conveying of materials, but also prevents the backflow of high-temperature synthesis gas, isolates oxygen to ensure the safety of feed, and participates in the thermal cracking reaction of carbon-containing raw materials W1 in the mobile filter bed V4.

[0058] Example 4: This example is basically the same as the previous example, except that this example provides a gasification process method of a fluidized bed coupled with a moving filter bed, including:

[0059] S1, adding carbonaceous raw material W1 to the moving filter bed V4 through the feeding device;

[0060] S2, introducing a gasifying agent into the fluidized bed gasifier V5 to generate a high-temperature raw synthesis gas containing fly ash;

[0061] S3, introducing high-temperature crude synthesis gas from the upper part of the moving filter bed V4;

[0062] By introducing the synthesis gas from the upper part of the mobile filter bed V4 and utilizing the downstream heat exchange between the synthesis gas and the carbon-containing raw material W1, the carbonized material at the lower part of the mobile filter bed V4 will catalytically crack the tar, thereby reducing the tar content in the purified synthesis gas W3 drawn out of the mobile filter bed V4. It is particularly suitable for the preparation of fuel gas (obtaining the most CO+H2+CH4) and is relatively suitable for the production of fuel gas (obtaining the most CO+H2+CH4).

[0063] S4, the mobile filter bed V4 absorbs and filters the fly ash, alkali metals and chlorine in the high-temperature raw synthesis gas through the carbon-containing raw material W1 to generate the purified synthesis gas W3;

[0064] S5, the carbonaceous raw material W1 in the mobile filter bed V4 is heated to 700-1000°C by the high-temperature crude synthesis gas in an oxygen-free environment, undergoing drying, pyrolysis and hydrocracking to generate pyrolysis gas and carbonized material;

[0065] S6, the purified synthesis gas W3 and the pyrolysis gas are drawn out from the top of the moving filter bed V4;

[0066] S7. The carbonized material is drawn out from the mobile filter bed V4 and used as raw material for the production of activated carbon.

[0067] A carbonized material outlet N1 is provided at the bottom of the mobile filter bed V4.

[0068] When the carbon-containing raw material W1 is biomass, it can be taken out from the mobile filter bed V4 through the carbonized material outlet N1 after pyrolysis and used as raw material for activated carbon production, thereby improving economic benefits.

[0069] Specifically, a dust collector discharge device V8 is provided between the cyclone dust collector V6 and the fluidized bed gasifier V5, for sending the fly ash captured by the cyclone dust collector V6 to the bottom of the fluidized bed gasifier V5 for further gasification.

[0070] The cyclone dust collector V6 uses centrifugal force to separate large fly ash particles from the high-temperature raw synthesis gas, and returns them to the bottom of the fluidized bed gasifier V5 for regasification through the dust collector discharge device V8.

[0071] Example 5: This example is basically the same as the previous example, except that the gasifying agent includes superheated steam W4 and oxygen / air W5, and the fluidized bed gasifier V5 is respectively provided with a distribution plate air intake control valve F8 and two central tube air intake control valves. The distribution plate air intake control valve F8 is used to control the gasifying agent from passing through the small holes of the distribution plate into the fluidized bed gasifier V5, and the central tube air intake control valve is used to control the gasifying agent from passing through the central tube into the fluidized bed gasifier V5.

[0072] The two central tube air inlet control valves are respectively the central tube superheated steam inlet control valve F9 and the central tube oxygen / air inlet control valve F10. The central tube superheated steam inlet control valve F9 is used to control the superheated steam W4 to flow into the fluidized bed gasifier V5 through the central tube, and the central tube oxygen / air inlet control valve F10 is used to control the oxygen / air W5 to flow into the fluidized bed gasifier V5 through the central tube;

[0073] The superheated steam W4 enters the fluidized bed gasifier V5 distribution plate through the distribution plate air inlet control valve F8 to maintain the fluidized state, and enters the central tube through the superheated steam control valve F9 to adjust the reaction temperature. The oxygen / air W5 enters the central tube through the oxygen / air control valve F10 to generate a high-temperature central jet, forming a central high-temperature zone to enhance the gasification reaction.

[0074] Specifically, a slag discharge buffer hopper V9 is provided at the bottom of the fluidized bed gasification furnace V5 for temporarily storing bottom slag discharged from the fluidized bed gasification furnace V5.

[0075] The bottom ash produced by the gasification work of the fluidized bed gasifier V5 will be discharged into the slag buffer hopper V9 through the bottom slag discharge port for temporary storage, which is convenient for subsequent external transportation and processing.

[0076] Example 6: This example is basically the same as the previous example, except that a gas distributor is provided in the mobile filter bed V4 for distributing the high-temperature raw synthesis gas introduced into the mobile filter bed V4, and the gas outlet of the gas distributor is provided downward.

[0077] The high-temperature crude synthesis gas enters the mobile filter bed V4 through the gas distributor. The gas distributor is provided with multiple downwardly arranged gas outlets to ensure that the high-temperature crude synthesis gas can be evenly distributed and pass through the filter bed. The gas outlet is set downward to prevent the carbon-containing materials falling downward from blocking the gas outlet.

[0078] The present invention introduces the high-ash, high-temperature crude synthesis gas produced by the fluidized bed gasifier V5 into the mobile filter bed V4, providing heat for the high-temperature pyrolysis of carbon-containing solid materials (coal, biomass, industrial carbon-containing waste, domestic waste, etc.) entering the mobile filter bed V4. The filtering and adsorption capabilities of the mobile filter bed V4 are utilized to filter and adsorb the high-ash, high-temperature crude synthesis gas, thereby removing impurities such as fly ash from the high-temperature crude synthesis gas. (For gasification raw materials such as biomass and domestic waste, harmful impurities such as alkali metals and chlorine will also be partially filtered and adsorbed.)

[0079] The clean crude synthesis gas and the pyrolysis gas generated by the pyrolysis of the mobile filter bed V4 enter the subsequent process sections; if the target product is fuel gas, the filtered crude synthesis gas and the pyrolysis gas generated by the pyrolysis of the mobile filter bed V4 can directly enter the waste heat recovery, water washing and other process sections; if the target product is a chemical product (methanol, ammonia, aviation kerosene, etc.), the filtered crude synthesis gas and the pyrolysis gas generated by the pyrolysis of the mobile filter bed V4 can enter the high-temperature POX furnace for high-temperature conversion, and methane and other gases are further converted into effective synthesis gas, and then enter the waste heat recovery, water washing and other process sections. The effective synthesis gas includes but is not limited to CO, H2 and other effective gases.

[0080] The coupled design of the fluidized bed gasifier V5 and the mobile filter bed V4 greatly reduces problems such as dust abrasion, alkali metal corrosion, and chlorine corrosion on subsequent system equipment, greatly improving equipment life and long-term operation capabilities.

[0081] The solid carbon-containing material in the mobile filter bed V4 is heated by high-temperature synthesis gas, dried, pyrolyzed and carbonized in a high-temperature, oxygen-free, high-hydrogen, high-steam environment. The carbonized solid material carries the fly ash filtered by adsorption and is continuously removed from the bottom of the mobile filter bed V4.

[0082] The present invention also includes a variety of process combinations:

[0083] For example, the scheme in which the raw synthesis gas directly enters the moving filter bed without passing through the cyclone separator, and the scheme in which the raw synthesis gas passes through multiple cyclone separators and then enters the moving filter bed are both specific forms of the present invention.

[0084] The clean synthesis gas after the mobile filter bed directly enters the waste heat recovery, water washing and other sections, or first enters the high-temperature POX furnace for high-temperature conversion and then enters the waste heat recovery, water washing and other sections. Both are specific process routes of the present invention.

[0085] The feeding method of the mobile filter bed material and the extraction method of the synthesis gas are also covered by the present invention. The material feeding scheme is top feeding, and schemes such as side feeding and top gas outlet are all specific forms of this patent.

[0086] The present invention only provides one method of distributing high-temperature synthesis gas into a moving filter bed. Other methods such as circular arrangement and "+"-shaped arrangement are also covered by this patent.

[0087] It is important to note that the construction and arrangement of the present application shown in a number of different exemplary embodiments are merely illustrative. Although only a few embodiments are described in detail in this disclosure, it should be readily understood by those who refer to this disclosure that many modifications are possible (e.g., the size, scale, structure, shape and proportion of various elements, as well as parameter values ​​(e.g., temperature, pressure, etc.), mounting arrangements, use of materials, color, directional changes, etc.) without departing substantially from the novel teachings and advantages of the subject matter described in this application. For example, an element shown as integrally formed may be composed of multiple parts or elements, the position of the element may be inverted or otherwise changed, and the nature or number or position of the discrete elements may be altered or changed. Therefore, all such modifications are intended to be included within the scope of the present invention. The order or sequence of any process or method steps may be changed or reordered according to alternative embodiments. In the claims, any "means plus function" clause is intended to cover the structure described herein that performs the function, and is not only structurally equivalent but also equivalent structures. Other replacements, modifications, changes, and omissions may be made in the design, operating conditions, and arrangement of the exemplary embodiments without departing from the scope of the present invention. Therefore, the invention is not limited to the specific embodiments, but extends to various modifications that still fall within the scope of the appended claims.

[0088] Additionally, in order to provide a concise description of exemplary embodiments, all features of an actual embodiment (i.e., those features that are not relevant to the best mode presently contemplated for carrying out the invention or those that are not relevant to implementing the invention) may not be described.

[0089] It will be appreciated that in the development of any actual embodiment, as in any engineering or design project, numerous implementation-specific decisions may be made. Such a development effort may be complex and time-consuming, but will, for those of ordinary skill having the benefit of this disclosure, be a routine undertaking of design, fabrication, and production without undue experimentation.

[0090] It should be noted that the above embodiments are only used to illustrate the technical solutions of the present invention and are not intended to limit the present invention. Although the present invention has been described in detail with reference to the preferred embodiments, those skilled in the art should understand that the technical solutions of the present invention may be modified or replaced by equivalents without departing from the spirit and scope of the technical solutions of the present invention, which should all be included in the scope of the claims of the present invention.

Claims

1. A gasification process of a fluidized bed coupled with a moving filter bed, characterized in that: include: S1, adding carbon-containing raw materials to the mobile filter bed through the feeding device; S2. introducing a gasifying agent into the fluidized bed gasifier to generate a high-temperature crude synthesis gas containing fly ash; S3, passing the high-temperature crude synthesis gas into a moving filter bed; S4, the mobile filter bed absorbs and filters fly ash, alkali metals, and chlorine in the high-temperature raw synthesis gas through the carbon-containing raw material to generate purified synthesis gas; S5. The carbon-containing raw materials in the mobile filter bed are heated to 700-1000°C by the high-temperature crude synthesis gas in an oxygen-free environment, undergoing drying, pyrolysis and hydrocracking to generate pyrolysis gas and carbonized material; S6, the purified synthesis gas and pyrolysis gas are led out through the moving filter bed; S7. The carbonized material is drawn out from the mobile filter bed as raw material for activated carbon production, or returned to the fluidized bed gasifier as gasification raw material.

2. The gasification process of a fluidized bed coupled with a moving filter bed according to claim 1, characterized in that: In step S3, before the high-temperature crude synthesis gas is passed into the mobile filter bed, the high-temperature crude synthesis gas is pre-dusted by a cyclone dust collector.

3. The gasification process of a fluidized bed coupled with a moving filter bed according to claim 1, characterized in that: The feeding device includes a silo, a lock hopper and a sending hopper. The output end of the silo is connected to the lock hopper input end through a lock hopper feed valve, the output end of the lock hopper is connected to the sending hopper input end through a sending hopper feed valve, and the output end of the sending hopper is connected to the top feed port of the mobile filter bed through a sending hopper discharge valve. A variable frequency feeder is arranged between the sending hopper discharge valve and the mobile filter bed.

4. The gasification process of a fluidized bed coupled with a moving filter bed according to claim 1, characterized in that: A carbonized material discharge port is provided at the bottom of the movable filter bed, and a movable bed discharge device is provided between the carbonized material discharge port and the fluidized bed gasifier for drawing out the carbonized material and sending it to the fluidized bed gasifier.

5. The gasification process of a fluidized bed coupled with a moving filter bed according to claim 3, characterized in that: The lock hopper is provided with a lock hopper pressure valve, the sending hopper is provided with a sending hopper pressure stabilizing valve, the moving filter bed is provided with a feed inlet protection gas valve, and the moving bed discharge device is provided with a moving bed return material conveying gas control valve, all of which are used to control the introduction of protective gas.

6. The gasification process of a fluidized bed coupled with a moving filter bed according to claim 1, characterized in that: A carbonized material outlet is provided at the bottom of the mobile filter bed.

7. The gasification process of a fluidized bed coupled with a moving filter bed according to claim 2, characterized in that: A dust collector discharging device is provided between the cyclone dust collector and the fluidized bed gasifier, for sending the fly ash captured by the cyclone dust collector to the bottom of the fluidized bed gasifier for re-gasification.

8. The gasification process of a fluidized bed coupled with a moving filter bed according to claim 1, characterized in that: The gasifying agent includes superheated steam and oxygen / air. The fluidized bed gasifier is respectively provided with a distribution plate air intake control valve and two central tube air intake control valves. The distribution plate air intake control valve is used to control the gasifying agent to pass into the fluidized bed gasifier through the small holes of the distribution plate, and the central tube air intake control valve is used to control the gasifying agent to pass into the fluidized bed gasifier through the central tube.

9. The gasification process of a fluidized bed coupled with a moving filter bed according to claim 1, characterized in that: A slag discharge buffer hopper is provided at the bottom of the fluidized bed gasification furnace for temporarily storing bottom slag discharged from the fluidized bed gasification furnace.

10. The gasification process of a fluidized bed coupled with a moving filter bed according to claim 1, characterized in that: A gas distributor is provided in the moving filter bed for distributing the high-temperature raw synthesis gas introduced into the moving filter bed.

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