Device and method for producing hydrogen by catalytic gasification of combined fluidized bed coal

Abstract

The present invention discloses a device and method for catalytic gasification of coal in a combined fluidized bed to produce hydrogen. A fluidized bed gasifier and a regeneration furnace are combined. The raw material inlet is located in the upper space of the fluidized bed gasifier. The return material outlet in the lower space of the fluidized bed gasifier is connected to the return material inlet of the regeneration furnace through a return material device. The upper outlet of the regeneration furnace is connected to the return material inlet in the upper space of the fluidized bed gasifier through a return material device. The technical solution mainly solves the problems of low hydrogen content, low carbon conversion rate, high energy consumption, etc. The device and method of the present invention preferably solve the above problems and can be applied to the field of coal-to-hydrogen production.

Description

Technical Field

[0001] The present invention belongs to the technical field of coal-to-hydrogen production, and relates to a device and method for catalytic gasification of coal to hydrogen in a combined fluidized bed, and particularly to a device and method for catalytic gasification hydrogen production reaction by combining a fluidized bed gasifier with a layered reaction and a fluidized bed regenerator. Background Art

[0002] As a clean energy, hydrogen energy has water as the final product during the energy conversion process, which can truly achieve zero emissions. It is widely used in aerospace power, vehicle fuel, fuel cells, combustion power generation, chemical production, etc., and plays an increasingly important role in the energy structure. Currently, the main methods for preparing hydrogen energy include partial oxidation reforming of heavy oil to produce hydrogen, electrolysis of water to produce hydrogen, and coal gasification to produce hydrogen, etc. Among them, coal gasification to produce hydrogen conforms to the energy structure characteristics and basic national conditions of our country, and is the mainstream hydrogen production technology. Traditional coal-to-hydrogen mainly includes processes such as coal gasification, gas purification, CO conversion, and purification. The equipment involved is numerous, and it is difficult to match the temperature and pressure between various equipment, resulting in high energy consumption, a long process, and a low system energy conversion rate. The gasification device is the key equipment for coal-to-hydrogen production. The existing gasification devices mainly use entrained flow beds and fluidized bed gasifiers, and the hydrogen content in the syngas at their outlets is generally low, increasing the load of subsequent purification, conversion, and purification processes.

[0003] Patent CN 101372312A proposes a method for producing hydrogen by coal gasification, which adopts a two-stage gasification method. The first step is to pyrolyze coal under the conditions of isolating air and not higher than 900 °C, mainly obtaining coal pyrolysis gasification, tar, and char. The coal pyrolysis gasification and tar are separated, and the obtained char enters the second step. Under the condition of not higher than 800 °C, it undergoes a gasification reaction with a gasifying agent, and the obtained char gas is purified to obtain the target product hydrogen. The problem with this method is that it is difficult to maintain the reaction temperature without external heat supply, and it is necessary to heat superheated steam to the temperature required for the gasification reaction, resulting in high energy consumption. In addition, the particle residence time is long and the carbon conversion rate is low, and the economic efficiency of industrial application is poor.

[0004] Patent CN 102585911A proposes a device and method for coal gasification to produce hydrogen. The reactor couples three processes: coal gasification, capture of carbon dioxide by a calcium-based adsorbent, and calcination of calcium carbonate. The carbon dioxide in the syngas from coal gasification is captured by the calcium-based adsorbent to increase the hydrogen content. However, the syngas at the outlet of the gasification reactor of this device needs to be cooled by an external heat exchanger before entering the adsorption reactor, and the temperature matching between the two reactors is poor. In addition, the coal ash entrained in the syngas is prone to cause pipeline blockage. The calcium-based adsorbent generated by the combustion reactor is divided into two streams and enters the gasification reactor and the adsorption reactor respectively. It is difficult to control the pressure balance and the proportion that cannot enter each section of the reactor, which is not conducive to controlling the effects of each reaction, thus affecting the outlet technical indicators. Summary of the Invention

[0005] In the above-mentioned technology, the promoting effect of the catalyst or the carrier on the reaction process in the gasifier is considered, which has a certain effect on increasing the hydrogen content in the syngas at the outlet. However, in terms of reaction process intensification, a reasonable and effective method has not been formed, and the catalysts or carriers used have not yet met the requirements of technical indicators and economy. Therefore, it is possible to consider intensifying the water-gas shift reaction and CO2 absorption reaction, and using a carrier with high catalytic performance to improve the coal catalytic gasification process for hydrogen production, generating high-quality hydrogen-rich syngas. Based on the above considerations, the water-gas shift reaction and carbonation reaction can be intensified in the gasifier, and a coal catalytic gasification technology for hydrogen production with a fast gasification reaction rate, a high degree of water-gas shift reaction, good catalytic reaction performance, simple process, stable operation and high efficiency can be studied.

[0006] One of the main technical problems to be solved by the present invention is the problems of low carbon conversion rate, low gasification intensity, low hydrogen production rate, high energy consumption and poor operation stability in the prior art. The present invention provides a combined fluidized bed coal catalytic gasification device for hydrogen production, which is composed of a fluidized bed gasifier and a fluidized bed regenerator. Raw coal A, oxidized high-temperature heat carrier G, gasifying agent of the upper gas distributor and gasifying agent of the lower gas distributor are introduced into the fluidized bed gasifier to carry out pyrolysis, gasification, water-gas shift reaction and carbonation reaction, generating hydrogen-rich syngas, gasified semicoke and carbonate carrier. The carbonate carrier and gasified semicoke enter the regenerator and carry out a high-temperature combustion reaction with oxygen-containing gas to decompose the carbonate carrier and regenerate the oxidized high-temperature heat carrier again. The cyclic regeneration of the high-temperature heat carrier is realized, the heat flow and material flow are balanced, and the gasification intensity, carbon conversion rate and hydrogen production rate are improved.

[0007] The second technical problem to be solved by the present invention is to provide a catalytic gasification reaction method corresponding to the solution of the first technical problem.

[0008] The first aspect of the present invention is to provide a device for combined fluidized bed coal catalytic gasification to produce hydrogen, including a fluidized bed gasifier, a raw material inlet, a lower gas distributor of the gasifier, an upper gas distributor of the gasifier, a gasifier outlet, a slag discharge port of the gasifier, a recycle outlet of the gasifier, a recycle device, a recycle inlet of the regeneration furnace, a regeneration furnace, a carrier feeding port, a gas distributor of the regeneration furnace, a gas outlet of the regeneration furnace, a slag discharge port of the regeneration furnace, a first cyclone separator, a hopper, a recycle straight pipe, a U-shaped recycle device, a recycle inlet of the gasifier, a heat recovery unit of the gasifier, a separation and purification unit, a second cyclone separator, and a cooling and purification unit of the regeneration furnace. Among them, the raw material inlet is connected to the fluidized bed gasifier, the fluidized bed gasifier is connected to the recycle device through the recycle outlet of the gasifier, the recycle device is connected to the regeneration furnace through the recycle inlet of the regeneration furnace, the carrier feeding port is connected to the regeneration furnace, the gas outlet of the regeneration furnace is connected to the first cyclone separator, the bottom of the first cyclone separator is connected to the hopper and the recycle straight pipe, the U-shaped recycle device is connected to the fluidized bed gasifier through the recycle inlet of the gasifier, the outlet of the first cyclone separator is connected to the second cyclone separator, the second cyclone separator is connected to the cooling and purification unit of the regeneration furnace, and the gas outlet of the gasifier is connected to the heat recovery unit of the gasifier and the separation and purification unit.

[0009] It is found that by optimizing the structure and process of the fluidized bed gasifier of the present invention, there are obvious advantages in strengthening the reaction process, material mass transfer, and heat transfer.

[0010] According to some embodiments of the present invention, the fluidized bed gasifier consists of an upper space and a lower space; the inner diameter of the upper space is greater than the inner diameter of the lower space; and / or, the height of the upper space is greater than or equal to the height of the lower space.

[0011] According to some embodiments of the present invention, the inner diameter of the upper space is 1.2 - 5.0 times the inner diameter of the lower space; and / or, the height of the upper space is 1.0 - 3.0 times the height of the lower space.

[0012] According to some embodiments of the present invention, the lower gas distributor of the gasifier is located at the bottom of the lower space of the fluidized bed gasifier, and forms an angle less than or equal to 60° with the horizontal axis. Air holes are provided on the conical surface of the lower gas distributor of the gasifier.

[0013] and / or, the upper gas distributor of the gasifier is located at the bottom of the upper space of the fluidized bed gasifier, and forms an angle less than or equal to 60° with the horizontal axis. Air holes are provided on the conical surface of the upper gas distributor of the gasifier.

[0014] According to some embodiments of the present invention, the lower gas distributor of the gasifier is located at the bottom of the lower space of the fluidized bed gasifier, forming an angle of 15-45° with the horizontal axis. The conical surface of the lower gas distributor of the gasifier is provided with air holes, and the air holes are evenly arranged along the circumference;

[0015] and / or, the upper gas distributor of the gasifier is located at the bottom of the upper space of the fluidized bed gasifier, forming an angle of 15-45° with the horizontal axis. The conical surface of the upper gas distributor of the gasifier is provided with air holes; the air holes are evenly arranged along the circumference.

[0016] According to some embodiments of the present invention, the lower gas distributor of the gasifier is provided with 5-50 circles of air holes, and the hole opening rate is 1-5%;

[0017] and / or, the upper gas distributor of the gasifier is provided with 10-100 circles of air holes, and the hole opening rate is 1-5%.

[0018] According to some embodiments of the present invention, the raw material inlet is located in the upper space of the fluidized bed gasifier, and the position is lower than 2 / 3 of the height of the upper space;

[0019] and / or, the return material outlet of the gasifier is located in the lower space of the fluidized bed gasifier;

[0020] and / or, the return material inlet of the gasifier is located in the upper space of the fluidized bed gasifier.

[0021] According to some embodiments of the present invention, the raw material inlet is located between 1 / 5 and 3 / 5 of the height of the upper space;

[0022] and / or, the return material outlet of the gasifier is located between 1 / 5 and 4 / 5 of the height of the lower space;

[0023] and / or, the return material inlet of the gasifier is located between 1 / 3 and 2 / 3 of the height of the upper space.

[0024] According to some embodiments of the present invention, the return material inlet of the regenerator is located below the regenerator, and the position is lower than 1 / 2 of the height of the regenerator;

[0025] and / or, the regenerator is provided with 1-5 carrier feeding ports, and the carrier feeding ports are located in the middle of the regenerator.

[0026] According to some embodiments of the present invention, the return material inlet of the regenerator is located between 1 / 5 and 1 / 2 of the height of the regenerator;

[0027] And / or, the regeneration furnace is provided with 1-5 carrier feeding ports, and the carrier feeding ports are located between 1 / 3 and 2 / 3 of the height of the regeneration furnace.

[0028] The second aspect of the present invention lies in providing a method for catalytic gasification of coal to produce hydrogen by using the device according to the first aspect, including the following main steps:

[0029] S1, The raw coal enters the upper space of the fluidized bed gasifier from the raw material inlet, and is mixed with water vapor from the lower gas distributor and the upper gas distributor of the gasifier and the oxidized high-temperature heat carrier from the gasifier return inlet, and undergoes catalytic pyrolysis, gasification and conversion reactions to produce syngas including H2, CO, CO2, and CH4; the oxidized high-temperature heat carrier further undergoes a carbonation reaction with CO2 in the syngas, absorbs CO2 in the syngas and generates a carbonate carrier;

[0030] S2, The syngas after the carbonation reaction passes through the gasifier heat recovery unit and the separation and purification unit (21) to obtain hydrogen-rich syngas;

[0031] S3, The carbonate carrier and gasification semicoke obtained in step S1 enter the regeneration furnace from the return device, and the gasification semicoke therein undergoes a high-temperature combustion reaction with oxygen-containing gas from the regeneration furnace gas distributor, decomposes the carbonate carrier, and regenerates the carbonate carrier to obtain an oxidized high-temperature heat carrier. The oxidized high-temperature heat carrier and fine ash are discharged from the top regeneration furnace gas outlet. The oxidized high-temperature heat carrier is separated in the first cyclone separator, and is circulated back to the upper space of the fluidized bed gasifier through the U-shaped return device via the gasifier return inlet. The fine ash is separated in the second cyclone separator, and the remaining flue gas is discharged after passing through the regeneration furnace cooling and purification unit.

[0032] The reaction temperature in the fluidized bed gasifier is 600-900°C, and the gas-phase linear velocity is 0.1-1.0 m / s; the reaction temperature in the regeneration furnace is 800-1200°C, and the gas-phase linear velocity is 1-10 m / s; the reaction pressure ranges in both the fluidized bed gasifier and the regeneration furnace are 0-2.0 MPa.

[0033] According to some embodiments of the present invention, water vapor is introduced into the lower gas distributor and the upper gas distributor of the gasifier, and the temperature of the water vapor is 200-800°C.

[0034] According to some embodiments of the present invention, steam is introduced into the lower gas distributor and the upper gas distributor of the gasifier. The proportion of the steam introduced into the upper gas distributor of the gasifier accounts for 10%-50% of the sum of the steam amounts in the upper gas distributor and the lower gas distributor of the gasifier.

[0035] According to some embodiments of the present invention, the molar ratio of the steam to the carbon in the raw coal, i.e., the H2O / C ratio, is 1.0-5.0 mol / mol.

[0036] According to some embodiments of the present invention, the oxygen-containing gas introduced into the regenerator gas distributor is selected from one or more of oxygen, air, and oxygen-enriched air.

[0037] According to some embodiments of the present invention, the molar ratio of the oxygen in the oxygen-containing gas to the carbon in the circulating semicoke, i.e., the O / C ratio, is greater than or equal to 1.5 mol / mol.

[0038] According to some embodiments of the present invention, the heat carrier is selected from natural ores; or a mixture of alkali metals, transition metals, and natural ores; or a mixture of alkali metals, transition metals, and alkaline earth metal Ca.

[0039] According to some embodiments of the present invention, the natural ore is limestone, dolomite, or olivine.

[0040] According to some embodiments of the present invention, the alkali metal, transition metal, or alkaline earth metal Ca is loaded on a carrier such as Al2O3, ZrO2, TiO2, or SiO2 in an amount of 0.1%-30% by weight of the active component in the catalyst by impregnation, dry mixing, or ion exchange methods.

[0041] A brief description of the process using the equipment of the present invention is as follows:

[0042] The raw coal enters the fluidized bed gasifier and is mixed and contacted with the gasifying agent from the upper gas distributor and the lower gas distributor of the gasifier to carry out pyrolysis, gasification, and shift reactions. The operating temperature is 600 - 900 °C, and the pressure is 0 - 2.0 MPa to produce syngas mainly composed of CO, H2, CO2, CH4, etc. The produced syngas further undergoes an intensified shift reaction with the steam in the gasifying agent from the upper gas distributor of the gasifier to increase the content of CO2 and H2 in the syngas. After the intensified shift reaction, the CO2 in the syngas reacts with the oxidized high-temperature heat carrier from the return material inlet of the gasifier to carry out a carbonation reaction to generate a carbonate carrier, which absorbs the CO2 in the syngas, and the hydrogen-rich syngas is discharged from the outlet of the fluidized bed gasifier. The carbonate carrier and the gasified semi-coke exit from the lower return material outlet of the gasifier and enter the regenerator through the return material device. The gasified semi-coke in the regenerator burns with the oxygen-containing gas from the gas distributor of the regenerator. The operating temperature is 800 - 1200 °C, and the pressure is 0 - 2.0 MPa to decompose the carbonate carrier to generate an oxidized high-temperature heat carrier and CO2. The entrained fine ash after combustion is discharged from the outlet of the regenerator and enters the first cyclone separator. The oxidized high-temperature heat carrier is separated and recycled back to the fluidized bed gasifier through the return straight pipe and the U-shaped return material device. The fine ash and flue gas enter the second cyclone separator and the regenerator cooling and purification unit.

[0043] Advantages of the present invention:

[0044] 1) A catalytic gasification hydrogen production device combining a fluidized bed gasifier and a regenerator is adopted. Pyrolysis, gasification, shift, and carbonation reactions are carried out in the fluidized bed gasifier, and the gasified semi-coke and the carbonate carrier then enter the regenerator for high-temperature combustion reactions, improving the carbon conversion rate and reaction intensity. The fluidized bed gasifier and the regenerator are relatively independent. The syngas at the outlet of the fluidized bed gasifier and the flue gas at the outlet of the regenerator are discharged from their respective pipelines. The syngas at the outlet of the fluidized bed gasifier contains almost no nitrogen, and the contents of CO2 and SO2 are relatively low, achieving the goals of high gasification efficiency and methane yield.

[0045] 2) The heat required for the pyrolysis and gasification reactions in the fluidized bed gasifier is provided by the oxidized high-temperature heat carrier generated by combustion in the regenerator and the heat released from its reaction with CO2, and the heat of the oxidized high-temperature heat carrier comes from the combustion heat release of the residual carbon in the gasified semi-coke, achieving a stable heat balance, and the process thermal efficiency and heat utilization rate are also more efficient than those of traditional gasification processes.

[0046] 3) The fluidized bed gasifier is divided into an upper space and a lower space. Steam is additionally introduced into the upper space to intensify the shift reaction process in the furnace, and the temperature in the upper space is slightly lower than that in the lower space, which can promote the balance of the shift reaction in the upper space and increase the hydrogen content. In addition, the inner diameter of the upper space is larger than that of the lower space, extending the residence time of the gas between the coal particles and promoting the gasification and shift reactions.

[0047] 4) The return material inlet of the gasifier is located in the upper space of the fluidized bed gasifier, in the middle area of the height of the upper space. After the oxidized high-temperature heat carrier enters the fluidized bed gasifier, it moves in a fluidized state from top to bottom to the lower space of the fluidized bed gasifier. It has a long mixing contact time with the gasified semicoke and the gasified syngas, with good material mixing effect, which is conducive to uniform heat and mass transfer and effectively promotes the pyrolysis, gasification, and carbonation reactions.

[0048] 5) The heat carrier used can be selected from inexpensive natural ores such as limestone, dolomite, and olivine; or a mixture of alkali metals, transition metals and natural ores, or a mixture of alkali metals, transition metals and alkaline earth metal Ca. According to 0.1 - 30% of the active component accounting for the mass of the catalyst, it is loaded on carriers such as Al2O3, ZrO2, TiO2, SiO2, etc. by methods such as impregnation, dry mixing, or ion exchange. The physical properties of the carrier and coal ash are quite different. The carrier and coal ash can complete the separation process in the regeneration furnace through combustion and simple separation equipment, solving the problem of difficult separation.

[0049] Adopting the technical solution of the present invention, through the combination of the fluidized bed gasifier and the regeneration furnace, catalytic pyrolysis, gasification, reforming, and carbonation reactions are carried out in the fluidized bed gasifier. The gasified semicoke and carbonate carrier are fed into the regeneration furnace for high-temperature combustion reaction, generating oxidized high-temperature heat carrier, coal ash, and flue gas. Among them, the oxidized high-temperature heat carrier is recycled back to the fluidized bed gasifier through the U-shaped return device, realizing the circulation of heat flow and material flow and achieving the purpose of full utilization. It can make the carbon conversion rate at the outlet of the device reach 95%, and the hydrogen content in the outlet syngas reach 80%. At the same time, it has the characteristics of large reaction intensity, high energy utilization rate, simple and compact structure, greatly reducing the equipment investment and production cost, and having good application prospects. BRIEF DESCRIPTION OF THE DRAWINGS

[0050] The drawings are used to provide further understanding of the present invention and constitute a part of the specification, and are used together with the embodiments of the present invention to explain the present invention, but do not constitute a limitation to the present invention. In the drawings:

[0051] Figure 1 It is a schematic diagram of the device process for combined fluidized bed coal catalytic gasification to produce hydrogen;

[0052] Figure 2 It is a schematic diagram of the structure of the lower-layer gas distributor of the gasifier, where a is the top view and b is the side view; the included angle in b is 45°;

[0053] Figure 3 It is a schematic diagram of the structure of the upper-layer gas distributor of the gasifier, where a is the top view and b is the side view; the included angle in b is 35°. DETAILED DESCRIPTION OF THE EMBODIMENTS

[0054] The present invention will be described in detail below with reference to the accompanying drawings and embodiments, but the present invention is not limited by the following embodiments.

[0055] Figure 1 Among them, 1 is a fluidized bed gasifier; 2 is a raw material inlet; 3 is a lower gas distributor of the gasifier; 4 is an upper gas distributor of the gasifier; 5 is a gasifier outlet; 6 is a slag discharge port of the gasifier; 7 is a return material outlet of the gasifier; 8 is a return material device; 9 is a return material inlet of the regenerator; 10 is a regenerator; 11 is a carrier feeding port; 12 is a gas distributor of the regenerator; 13 is a regenerator outlet; 14 is a slag discharge port of the regenerator; 15 is a first cyclone separator; 16 is an ash hopper; 17 is a return material straight pipe; 18 is a U-shaped return material device; 19 is a return material inlet of the gasifier; 20 is a heat recovery unit of the gasifier; 21 is a separation and purification unit; 22 is a second cyclone separator; 23 is a cooling and purification unit of the regenerator. A is raw coal; B is carbonate carrier + gasification ash slag; C is carbonate carrier + gasification semicoke; D is return material gas; E is supplementary carrier; F is combustion ash slag; G is oxidized regenerated heat carrier; H is fine ash; I is flue gas; J is tar; K is hydrogen-rich syngas.

[0056] The raw coal A enters the fluidized bed gasifier 1 through the raw material inlet 2, and is mixed and contacted with the gasifying agent (steam) from the upper gas distributor 4 and the lower gas distributor 3 of the gasifier, and undergoes pyrolysis, gasification, and shift reactions to produce synthesis gas such as CO, H2, CO2, and CH4. The produced synthesis gas further undergoes an intensified shift reaction with the steam in the upper gas distributor 4 of the gasifier to increase the content of CO2 and H2 in the synthesis gas. After the intensified shift reaction, CO2 in the synthesis gas undergoes a carbonation reaction with the oxidized high-temperature heat carrier from the return material inlet 19 of the gasifier to absorb CO2 in the synthesis gas. The hydrogen-rich syngas is discharged from the fluidized bed gasifier outlet 5 and enters the heat recovery unit 20 and the separation and purification unit 21 of the gasifier. The carbonate carrier and the gasification semicoke C leave the fluidized bed gasifier 1 from the lower return material outlet 7 of the gasifier and enter the regenerator 10 through the return material device 8. The gasification semicoke in the regenerator 10 burns with the oxygen-containing gas from the gas distributor 12 of the regenerator, decomposes the carbonate carrier, generates an oxidized high-temperature heat carrier and CO2, and the entrained fine ash after combustion is discharged from the regenerator outlet 13 and enters the first cyclone separator 15. The oxidized high-temperature heat carrier G is separated and circulated back to the fluidized bed gasifier 1 through the return material straight pipe 17 and the U-shaped return material device 18, and the fine ash and flue gas enter the second cyclone separator 22 and the cooling and purification unit 23 of the regenerator.

[0057]

Example 1

[0058] Adopt Figure 1A combined fluidized bed coal catalytic gasification hydrogen production device as shown. The inner diameter of the lower space of the fluidized bed gasifier is 1.0 m, and the height of the lower space is 3 m. The inner diameter of the upper space of the fluidized bed gasifier is 2 m, and the height of the upper space is 6 m. The height of the raw material inlet is located at 1 / 2 of the height of the fluidized bed gasifier. The return material inlet of the regenerator is located at 2 / 3 of the height of the fluidized bed gasifier. The return material outlet of the gasifier is located at 1 / 4 of the height of the fluidized bed gasifier. The return material inlet of the gasifier is located at 3 / 5 of the height of the fluidized bed gasifier. The inner diameter of the regenerator is 1.2 m, and the height is 15 mm. The return material inlet of the regenerator is located at 1 / 10 of the height of the regenerator.

[0059] Inner Mongolia lignite is selected as the raw material and added into the fluidized bed gasifier from the raw material inlet. High-temperature steam at 500 °C is introduced into the upper gas distributor and the lower gas distributor of the fluidized bed. The proportion of the steam introduced into the upper gas distributor of the gasifier accounts for 30% of the sum of the steam amounts in the upper gas distributor and the lower gas distributor of the gasifier, and the water-carbon ratio is 3.0 mol / mol. The CaO high-temperature heat carrier enters the fluidized bed gasifier from the gasifier return material inlet. Multiple streams of materials are mixed and contacted to carry out pyrolysis, gasification, water-gas shift and carbonation reactions. The operating temperature of the fluidized bed gasifier is 600 °C, and the operating pressure is atmospheric pressure. Carbonate carrier, semi-coke and syngas rich in hydrogen are generated. The H2 content in the outlet syngas is 80%. The carbonate carrier and partially gasified semi-coke enter the regenerator through the return material device and carry out combustion reaction with the air from the gas distributor of the regenerator. The operating temperature is 1000 °C, and the operating pressure is atmospheric pressure. The oxygen-carbon ratio is 2.0 mol / mol. The carbonate carrier is decomposed into oxidized high-temperature heat carrier and CO2. The oxidized high-temperature heat carrier is separated, collected and circulated into the fluidized bed gasifier through the first cyclone separator, the downcomer and the U-shaped return material device, providing sensible heat and oxygen carrier for the pyrolysis and gasification reactions in the fluidized bed gasifier. The carbon conversion rate at the outlet of the regenerator reaches 95%.

[0060]

Example 2

[0061] Adopt Figure 1 A combined fluidized bed coal catalytic gasification hydrogen production device as shown. The inner diameter of the lower space of the fluidized bed gasifier is 1.0 m, and the height of the lower space is 3 m. The inner diameter of the upper space of the fluidized bed gasifier is 3 m, and the height of the upper space is 6 m. The height of the raw material inlet is located at 1 / 2 of the height of the fluidized bed gasifier. The return material inlet of the regenerator is located at 2 / 3 of the height of the fluidized bed gasifier. The return material outlet of the gasifier is located at 1 / 4 of the height of the fluidized bed gasifier. The return material inlet of the gasifier is located at 3 / 5 of the height of the fluidized bed gasifier. The inner diameter of the regenerator is 1.2 m, and the height is 15 mm. The return material inlet of the regenerator is located at 1 / 10 of the height of the regenerator.

[0062] Inner Mongolia lignite is selected as the raw material and added into the fluidized bed gasifier from the raw material inlet. High-temperature steam at 500 °C is introduced into the upper gas distributor and the lower gas distributor of the fluidized bed. The proportion of steam introduced into the upper gas distributor of the gasifier accounts for 30% of the sum of the steam amounts in the upper gas distributor and the lower gas distributor of the gasifier, and the water-carbon ratio is 3.0 mol / mol. The CaO high-temperature heat carrier enters the fluidized bed gasifier from the return inlet of the gasifier. Multiple streams of materials are mixed and contacted to carry out pyrolysis, gasification, shift, and carbonation reactions. The operating temperature of the fluidized bed gasifier is 620 °C, and the operating pressure is atmospheric pressure. Carbonate carriers, char, and syngas rich in hydrogen are generated. The H2 content in the outlet syngas is 82%. The carbonate carriers and gasified char enter the regenerator through the return device and carry out a combustion reaction with the air from the gas distributor of the regenerator. The operating temperature is 1000 °C, and the operating pressure is atmospheric pressure. The oxygen-carbon ratio is 2.0 mol / mol. The carbonate carriers are decomposed into oxidized high-temperature heat carriers and CO2. The oxidized high-temperature heat carriers are separated, collected, and circulated into the fluidized bed gasifier through the first cyclone separator, the downcomer, and the U-shaped return device, providing sensible heat and oxygen carriers for the pyrolysis and gasification reactions in the fluidized bed gasifier. The carbon conversion rate at the outlet of the regenerator reaches 95%.

[0063]

Example 3

[0064] Adopt Figure 1 A combined fluidized bed coal catalytic gasification hydrogen production device as shown. The inner diameter of the lower space of the fluidized bed gasifier is 1.0 m, and the height of the lower space is 3 m. The inner diameter of the upper space of the fluidized bed gasifier is 2 m, and the height of the upper space is 6 m. The height of the raw material inlet is located at 1 / 2 of the height of the fluidized bed gasifier. The return inlet of the regenerator is located at 2 / 3 of the height of the fluidized bed gasifier. The return outlet of the gasifier is located at 1 / 4 of the height of the fluidized bed gasifier. The return inlet of the gasifier is located at 3 / 5 of the height of the fluidized bed gasifier. The inner diameter of the regenerator is 1.2 m, and the height is 15 mm. The return inlet of the regenerator is located at 1 / 10 of the height of the regenerator.

[0065] Inner Mongolia lignite is selected as the raw material and added into the fluidized bed gasifier from the raw material inlet. High-temperature steam at 500 °C is introduced into the upper gas distributor and the lower gas distributor of the fluidized bed. The proportion of steam introduced into the upper gas distributor of the gasifier accounts for 50% of the sum of the steam amounts in the upper gas distributor and the lower gas distributor of the gasifier, and the water-carbon ratio is 3.0 mol / mol. The CaO high-temperature heat carrier enters the fluidized bed gasifier from the return inlet of the gasifier. Multiple streams of materials are mixed and contacted to carry out pyrolysis, gasification, shift, and carbonation reactions. The operating temperature of the fluidized bed gasifier is 600 °C, and the operating pressure is atmospheric pressure. Carbonate carriers, char, and syngas rich in hydrogen are generated. The H2 content in the outlet syngas is 85%. The carbonate carriers and gasified char enter the regenerator through the return device and carry out a combustion reaction with the air from the gas distributor of the regenerator. The operating temperature is 1000 °C, and the operating pressure is atmospheric pressure. The oxygen-carbon ratio is 2.0 mol / mol. The carbonate carriers are decomposed into oxidized high-temperature heat carriers and CO2. The oxidized high-temperature heat carriers are separated, collected, and circulated into the fluidized bed gasifier through the first cyclone separator, the downcomer straight pipe, and the U-shaped return device, providing sensible heat and oxygen carriers for the pyrolysis and gasification reactions in the fluidized bed gasifier. The carbon conversion rate at the outlet of the regenerator reaches 95%.

[0066]

Example 4

[0067] Adopt Figure 1 A combined fluidized bed coal catalytic gasification hydrogen production device as shown. The inner diameter of the lower space of the fluidized bed gasifier is 1.0 m, and the height of the lower space is 3 m. The inner diameter of the upper space of the fluidized bed gasifier is 2 m, and the height of the upper space is 6 m. The height of the raw material inlet is located at 1 / 2 of the height of the fluidized bed gasifier. The return inlet of the regenerator is located at 2 / 3 of the height of the fluidized bed gasifier. The return outlet of the gasifier is located at 1 / 4 of the height of the fluidized bed gasifier. The return inlet of the gasifier is located at 3 / 5 of the height of the fluidized bed gasifier. The inner diameter of the regenerator is 1.2 m, and the height is 15 mm. The return inlet of the regenerator is located at 1 / 10 of the height of the regenerator.

[0068] Inner Mongolia lignite is selected as the raw material and added into the fluidized bed gasifier from the raw material inlet. High-temperature steam at 500 °C is introduced into the upper gas distributor and the lower gas distributor of the fluidized bed. The proportion of steam introduced into the upper gas distributor of the gasifier accounts for 30% of the sum of the steam amounts in the upper gas distributor and the lower gas distributor of the gasifier, and the water-carbon ratio is 3.0 mol / mol. The CaO high-temperature heat carrier enters the fluidized bed gasifier from the recycle inlet of the gasifier. Multiple streams of materials are mixed and contacted to carry out pyrolysis, gasification, shift, and carbonation reactions. The operating temperature of the fluidized bed gasifier is 600 °C, and the operating pressure is atmospheric pressure. Carbonate carriers, char, and syngas rich in hydrogen are generated. The H2 content in the outlet syngas is 80%. The carbonate carriers and gasified char enter the regenerator through the recycle device and carry out a combustion reaction with the air from the gas distributor of the regenerator. The operating temperature is 1100 °C, and the operating pressure is atmospheric pressure. The oxygen-carbon ratio is 2.5 mol / mol. The carbonate carriers are decomposed into oxidized high-temperature heat carriers and CO2. The oxidized high-temperature heat carriers are separated, collected, and recycled into the fluidized bed gasifier through the first cyclone separator, the downcomer, and the U-shaped recycle device, providing sensible heat and oxygen carriers for the pyrolysis and gasification reactions in the fluidized bed gasifier. The carbon conversion rate at the outlet of the regenerator reaches 99%.

[0069]

Example 5

[0070] Adopt Figure 1 A combined fluidized bed coal catalytic gasification hydrogen production device as shown. The inner diameter of the lower space of the fluidized bed gasifier is 1.0 m, and the height of the lower space is 3 m. The inner diameter of the upper space of the fluidized bed gasifier is 2 m, and the height of the upper space is 6 m. The height of the raw material inlet is located at 1 / 2 of the height of the fluidized bed gasifier. The recycle inlet of the regenerator is located at 2 / 3 of the height of the fluidized bed gasifier. The recycle outlet of the gasifier is located at 1 / 4 of the height of the fluidized bed gasifier. The recycle inlet of the gasifier is located at 3 / 5 of the height of the fluidized bed gasifier. The inner diameter of the regenerator is 1.2 m, and the height is 15 mm. The recycle inlet of the regenerator is located at 1 / 10 of the height of the regenerator.

[0071] Inner Mongolia lignite is selected as the raw material and added into the fluidized bed gasifier from the raw material inlet. High-temperature steam at 500 °C is introduced into the upper gas distributor and the lower gas distributor of the fluidized bed. The proportion of steam introduced into the upper gas distributor of the gasifier accounts for 30% of the sum of the steam amounts in the upper gas distributor and the lower gas distributor of the gasifier, and the water-carbon ratio is 2.0 mol / mol. The CaO high-temperature heat carrier enters the fluidized bed gasifier from the return inlet of the gasifier. Multiple streams of materials are mixed and contacted to carry out pyrolysis, gasification, shift, and carbonation reactions. The operating temperature of the fluidized bed gasifier is 600 °C, and the operating pressure is atmospheric pressure. Carbonate carriers, char, and syngas rich in hydrogen are generated. The H2 content in the outlet syngas is 73%. The carbonate carriers and gasified char enter the regenerator through the return device and carry out a combustion reaction with the air from the gas distributor of the regenerator. The operating temperature is 1100 °C, and the operating pressure is atmospheric pressure. The oxygen-carbon ratio is 2.5 mol / mol. The carbonate carriers are decomposed into oxidized high-temperature heat carriers and CO2. The oxidized high-temperature heat carriers are separated, collected, and circulated into the fluidized bed gasifier through the first cyclone separator, the downcomer straight pipe, and the U-shaped return device, providing sensible heat and oxygen carriers for the pyrolysis and gasification reactions in the fluidized bed gasifier. The carbon conversion rate at the outlet of the regenerator reaches 96%.

[0072]

Example 6

[0073] Adopt Figure 1 A combined fluidized bed coal catalytic gasification hydrogen production device as shown. The inner diameter of the lower space of the fluidized bed gasifier is 1.0 m, and the height of the lower space is 3 m. The inner diameter of the upper space of the fluidized bed gasifier is 2 m, and the height of the upper space is 6 m. The height of the raw material inlet is located at 1 / 2 of the height of the fluidized bed gasifier. The return inlet of the regenerator is located at 2 / 3 of the height of the fluidized bed gasifier. The return outlet of the gasifier is located at 1 / 4 of the height of the fluidized bed gasifier. The return inlet of the gasifier is located at 3 / 5 of the height of the fluidized bed gasifier. The inner diameter of the regenerator is 1.2 m, and the height is 15 mm. The return inlet of the regenerator is located at 1 / 10 of the height of the regenerator.

[0074] Inner Mongolia lignite is selected as the raw material and added into the fluidized bed gasifier from the raw material inlet. High-temperature steam at 500 °C is introduced into the upper gas distributor and the lower gas distributor of the fluidized bed. The proportion of steam introduced into the upper gas distributor of the gasifier accounts for 30% of the sum of the steam amounts in the upper gas distributor and the lower gas distributor of the gasifier, and the water-carbon ratio is 3.0 mol / mol. The CaO high-temperature heat carrier loaded with K2CO3 enters the fluidized bed gasifier from the return inlet of the gasifier. Multiple streams of materials are mixed and contacted to carry out pyrolysis, gasification, shift, and carbonation reactions. The operating temperature of the fluidized bed gasifier is 600 °C, and the operating pressure is atmospheric pressure. Carbonate carriers, char, and syngas rich in hydrogen are generated. The H2 content in the outlet syngas is 90%. The carbonate carriers and gasified char enter the regeneration furnace through the return device and carry out a combustion reaction with the air from the gas distributor of the regeneration furnace. The operating temperature is 1000 °C, and the operating pressure is atmospheric pressure. The oxygen-carbon ratio is 2.0 mol / mol. The carbonate carriers are decomposed into oxidized high-temperature heat carriers and CO2. The oxidized high-temperature heat carriers are separated, collected, and circulated into the fluidized bed gasifier through the first cyclone separator, the downcomer, and the U-shaped return device, providing sensible heat and oxygen carriers for the pyrolysis and gasification reactions in the fluidized bed gasifier. The carbon conversion rate at the outlet of the regeneration furnace reaches 99%.

[0075]

Example 7

[0076] Adopt Figure 1 A combined fluidized bed coal catalytic gasification hydrogen production device as shown. The inner diameter of the lower space of the fluidized bed gasifier is 1.0 m, and the height of the lower space is 3 m. The inner diameter of the upper space of the fluidized bed gasifier is 2 m, and the height of the upper space is 6 m. The height of the raw material inlet is located at 1 / 2 of the height of the fluidized bed gasifier. The return inlet of the regeneration furnace is located at 2 / 3 of the height of the fluidized bed gasifier. The return outlet of the gasifier is located at 1 / 4 of the height of the fluidized bed gasifier. The return inlet of the gasifier is located at 1 / 5 of the height of the fluidized bed gasifier. The inner diameter of the regeneration furnace is 1.2 m, and the height is 15 mm. The return inlet of the regeneration furnace is located at 1 / 10 of the height of the regeneration furnace.

[0077] Inner Mongolia lignite is selected as the raw material and added into the fluidized bed gasifier from the raw material inlet. High-temperature steam at 500 °C is introduced into the upper gas distributor and the lower gas distributor of the fluidized bed. The proportion of steam introduced into the upper gas distributor of the gasifier accounts for 30% of the sum of the steam amounts in the upper gas distributor and the lower gas distributor of the gasifier, and the water-carbon ratio is 3.0 mol / mol. The CaO high-temperature heat carrier enters the fluidized bed gasifier from the gasifier return inlet. Multiple streams of materials are mixed and contacted to carry out pyrolysis, gasification, shift, and carbonation reactions. The operating temperature of the fluidized bed gasifier is 600 °C, and the operating pressure is atmospheric pressure. Carbonate carrier, char, and syngas rich in hydrogen are generated. Due to the relatively low position of the gasifier return inlet, the mixing contact time of the materials is short and the mixing effect is poor. The H2 content in the syngas at the outlet is 70%. The carbonate carrier and gasified char enter the regenerator through the return device and carry out a combustion reaction with the air from the gas distributor of the regenerator. The operating temperature is 1000 °C, and the operating pressure is atmospheric pressure. The oxygen-carbon ratio is 2.0 mol / mol. The carbonate carrier is decomposed into the oxidized high-temperature heat carrier and CO2. The oxidized high-temperature heat carrier is separated, collected, and circulated into the fluidized bed gasifier through the first cyclone separator, the downcomer, and the U-shaped return device, providing sensible heat and oxygen carrier for the pyrolysis and gasification reactions in the fluidized bed gasifier. The carbon conversion rate at the outlet of the regenerator reaches 95%.

[0078]

Example 8

[0079] Adopt Figure 1 A combined fluidized bed coal catalytic gasification hydrogen production device as shown. The inner diameter of the lower space of the fluidized bed gasifier is 1.0 m, and the height of the lower space is 3 m. The inner diameter of the upper space of the fluidized bed gasifier is 2 m, and the height of the upper space is 6 m. The height of the raw material inlet is located at 1 / 2 of the height of the fluidized bed gasifier. The regenerator return inlet is located at 2 / 3 of the height of the fluidized bed gasifier. The gasifier return outlet is located at 1 / 4 of the height of the fluidized bed gasifier. The gasifier return inlet is located at 3 / 5 of the height of the fluidized bed gasifier. The inner diameter of the regenerator is 1.2 m, and the height is 15 mm. The regenerator return inlet is located at 1 / 10 of the height of the regenerator.

[0080] Inner Mongolia lignite is selected as the raw material and fed into the fluidized bed gasifier from the raw material inlet. High-temperature steam at 500 °C is introduced into the gas distributor at the bottom of the lower space of the fluidized bed gasifier, and the water-carbon ratio is 3.0 mol / mol. The CaO high-temperature heat carrier loaded with K2CO3 enters the fluidized bed gasifier from the return feed inlet of the gasifier. Multiple streams of materials are mixed and contacted to carry out pyrolysis, gasification, shift, and carbonation reactions. The operating temperature of the fluidized bed gasifier is 600 °C, and the operating pressure is atmospheric pressure. Carbonate carrier, semi-coke, and syngas rich in hydrogen are generated, and the H2 content in the outlet syngas is 70%. The carbonate carrier and gasified semi-coke enter the regeneration furnace through the return feed device and carry out a combustion reaction with the air from the gas distributor of the regeneration furnace. The operating temperature is 1000 °C, the operating pressure is atmospheric pressure, and the oxygen-carbon ratio is 2.0 mol / mol. The carbonate carrier is decomposed into the oxidized high-temperature heat carrier and CO2. The oxidized high-temperature heat carrier is separated, collected, and circulated into the fluidized bed gasifier through the first cyclone separator, downcomer, and U-shaped return feed device, providing sensible heat and oxygen carrier for the pyrolysis and gasification reactions in the fluidized bed gasifier. The carbon conversion rate at the outlet of the regeneration furnace reaches 92%.

[0081]

Example 9

[0082] Adopt Figure 1 A combined fluidized bed coal catalytic gasification hydrogen production device as shown. The inner diameter of the lower space of the fluidized bed gasifier is 1.0 m, and the height of the lower space is 3 m. The inner diameter of the upper space of the fluidized bed gasifier is 2 m, and the height of the upper space is 6 m. The height of the raw material inlet is located at 1 / 2 of the height of the fluidized bed gasifier. The return feed inlet of the regeneration furnace is located at 2 / 3 of the height of the fluidized bed gasifier. The return feed outlet of the gasifier is located at 1 / 4 of the height of the fluidized bed gasifier. The return feed inlet of the gasifier is located at 3 / 5 of the height of the fluidized bed gasifier. The inner diameter of the regeneration furnace is 1.2 m, and the height is 15 mm. The return feed inlet of the regeneration furnace is located at 1 / 10 of the height of the regeneration furnace.

[0083] Inner Mongolia lignite is selected as the raw material and added into the fluidized bed gasifier from the raw material inlet. High-temperature steam at 500 °C is introduced into the gas distributor at the bottom of the upper space of the fluidized bed gasifier, and the steam-carbon ratio is 3.0 mol / mol. The CaO high-temperature heat carrier loaded with K2CO3 enters the fluidized bed gasifier from the recycle inlet of the gasifier. Multiple streams of materials are mixed and contacted to carry out pyrolysis, gasification, shift, and carbonation reactions. The operating temperature of the fluidized bed gasifier is 600 °C, and the operating pressure is atmospheric pressure. Carbonate carriers, semicoke, and syngas rich in hydrogen are generated, and the H2 content in the outlet syngas is 50%. The carbonate carriers and gasified semicoke enter the regeneration furnace through the recycle device and carry out combustion reactions with the air from the gas distributor of the regeneration furnace. The operating temperature is 1000 °C, the operating pressure is atmospheric pressure, and the oxygen-carbon ratio is 2.0 mol / mol. The carbonate carriers are decomposed into oxidized high-temperature heat carriers and CO2. The oxidized high-temperature heat carriers are separated, collected, and recycled into the fluidized bed gasifier through the first cyclone separator, downcomer, and U-shaped recycle device, providing sensible heat and oxygen carriers for the pyrolysis and gasification reactions in the fluidized bed gasifier. The carbon conversion rate at the outlet of the regeneration furnace reaches 70%.

[0084]

Comparative Example 1

[0085] For the coal gasification reaction device in the traditional coal-to-hydrogen process, taking the Shell entrained flow gasifier as an example, the selected coal type is lignite, the operating pressure is 3.0 MPa, and the average operating temperature is 1800 °C. The H2 content in the outlet gas composition is 30%, and the carbon conversion rate is 98%.

[0086]

Comparative Example 2

[0087] For the coal gasification reaction device in the traditional coal-to-hydrogen process, taking the Winkler fluidized bed gasifier as an example, the selected coal type is lignite, the operating pressure is 3.0 MPa, and the average operating temperature is 1000 °C. The H2 content in the outlet gas composition is 33%, and the carbon conversion rate is 90%.

[0088]

Comparative Example 3

[0089] For the gasification reaction device in the multi-layer fluidized bed catalytic gasification process proposed by ENN Group, Inner Mongolia lignite is selected as the raw material, loaded with 15% potassium carbonate catalyst, the operating pressure is 2.5 MPa, and the operating temperature is 700 °C. The hydrogen content in the outlet gas composition is 43%, and the carbon conversion rate is 50%.

[0090] The parameter comparison between the examples and comparative examples is shown in Table 1.

[0091]

[0092] It should be noted that the above-described embodiments are only used to explain the present invention and do not constitute any limitation to the present invention. The present invention has been described by referring to typical embodiments, but it should be understood that the words used therein are descriptive and explanatory words rather than limiting words. Modifications can be made to the present invention within the scope of the claims of the present invention as stipulated, and the present invention can be revised without departing from the scope and spirit of the present invention. Although the present invention described therein relates to specific methods, materials and embodiments, it does not mean that the present invention is limited to the specific examples disclosed therein. On the contrary, the present invention can be extended to all other methods and applications with the same functions.

Claims

1. A method for hydrogen production by catalytic gasification of coal according to an apparatus for catalytic gasification of coal in a combined fluidized bed, characterized in that, The device for combined fluidized bed coal catalytic gasification to produce hydrogen includes a fluidized bed gasifier (1), a raw material inlet (2), a lower gas distributor of the gasifier (3), an upper gas distributor of the gasifier (4), a gasifier outlet (5), a slag discharge port of the gasifier (6), a return material outlet of the gasifier (7), a return material device (8), a return material inlet of the regeneration furnace (9), a regeneration furnace (10), a carrier feeding port (11), a gas distributor of the regeneration furnace (12), a gas outlet of the regeneration furnace (13), a slag discharge port of the regeneration furnace (14), a first cyclone separator (15), a hopper (16), a return material straight pipe (17), a U-shaped return material device (18), a return material inlet of the gasifier (19), a heat recovery unit of the gasifier (20), a separation and purification unit (21), a second cyclone separator (22), and a cooling and purification unit of the regeneration furnace (23). The raw material inlet (2) is connected to the fluidized bed gasifier (1). The fluidized bed gasifier (1) is connected to the return material device (8) through the return material outlet of the gasifier (7). The return material device (8) is connected to the regeneration furnace (10) through the return material inlet of the regeneration furnace (9). The carrier feeding port (11) is connected to the regeneration furnace (10). The gas outlet of the regeneration furnace (13) is connected to the first cyclone separator (15). The bottom of the first cyclone separator (15) is connected to the hopper (16) and the return material straight pipe (17). The U-shaped return material device (18) is connected to the fluidized bed gasifier (1) through the return material inlet of the gasifier (19). The outlet of the first cyclone separator (15) is connected to the second cyclone separator (22). The second cyclone separator (22) is connected to the cooling and purification unit of the regeneration furnace (23). The gasifier outlet (5) is connected to the heat recovery unit of the gasifier (20) and the separation and purification unit (21). The fluidized bed gasifier (1) consists of an upper space and a lower space. The inner diameter of the upper space is larger than that of the lower space, and the height of the upper space is greater than or equal to the height of the lower space. The lower gas distributor of the gasifier (3) is located at the bottom of the lower space of the fluidized bed gasifier (1), with an angle less than or equal to 60° with the horizontal axis. The conical surface of the lower gas distributor of the gasifier (3) is provided with air holes. The upper gas distributor of the gasifier (4) is located at the bottom of the upper space of the fluidized bed gasifier (1), with an angle less than or equal to 60° with the horizontal axis. The conical surface of the upper gas distributor of the gasifier (4) is provided with air holes. The raw material inlet (2) is located within the upper space of the fluidized bed gasifier (1), and its position is lower than 2 / 3 of the height of the upper space. The return material outlet of the gasifier (7) is located within the lower space of the fluidized bed gasifier (1). The return material inlet of the gasifier (19) is located within the upper space of the fluidized bed gasifier (1). The method includes the following main steps: S1. The raw coal (A) enters the upper space of the fluidized bed gasifier (1) from the raw material inlet (2), mixes with the steam from the lower gas distributor (3) and the upper gas distributor (4) of the gasifier and the oxidized high-temperature heat carrier (G) from the gasifier return inlet (19), and undergoes catalytic pyrolysis, gasification and shift reactions to produce syngas including H2, CO, CO2 and CH4. The oxidized high-temperature heat carrier (G) then undergoes a carbonation reaction with CO2 in the syngas, absorbs CO2 in the syngas and generates a carbonate carrier. S2. The syngas after the carbonation reaction passes through the gasifier heat recovery unit (20) and the separation and purification unit (21) to obtain hydrogen-rich syngas (K). S3. The carbonate carrier and the gasification semicoke (C) obtained in step S1 enter the regeneration furnace (10) from the return device (8). The gasification semicoke therein undergoes a high-temperature combustion reaction with the oxygen-containing gas from the regeneration furnace gas distributor (12) to decompose the carbonate carrier, and the carbonate carrier is regenerated to obtain the oxidized high-temperature heat carrier (G). The oxidized high-temperature heat carrier (G) and the fine ash (H) are discharged from the top regeneration furnace gas outlet (13). The oxidized high-temperature heat carrier (G) is separated in the first cyclone separator (15), and is circulated back to the upper space of the fluidized bed gasifier (1) through the U-shaped return device (18) via the gasifier return inlet (19). The fine ash (H) is separated in the second cyclone separator (22), and the remaining flue gas (I) is discharged after passing through the regeneration furnace cooling and purification unit (23). Steam is introduced into the lower gas distributor (3) and the upper gas distributor (4) of the gasifier, and the temperature of the steam is 200 - 800 °C. The proportion of the steam introduced by the upper gas distributor (4) of the gasifier accounts for 30% - 50% of the sum of the steam amounts of the upper gas distributor (4) and the lower gas distributor (3) of the gasifier.

2. The method according to claim 1, characterized in that, The inner diameter of the upper space is 1.2 - 5.0 times that of the lower space; and / or, the height of the upper space is 1.0 - 3.0 times that of the lower space.

3. The method according to claim 1 or 2, characterized in that The lower gas distributor (3) of the gasifier forms an angle of 15 - 45° with the horizontal axis. And / or, the air holes provided on the conical surface of the lower gas distributor (3) of the gasifier are evenly arranged in a circumferential direction. And / or, there are 5 - 50 circles of air holes provided on the conical surface of the lower gas distributor (3) of the gasifier, and the aperture ratio is 1% - 5%. And / or, the upper gas distributor (4) of the gasifier forms an angle of 15 - 45° with the horizontal axis. And / or, the air holes provided on the conical surface of the upper gas distributor (4) of the gasifier are evenly arranged in a circumferential direction. And / or, there are 10 - 100 circles of air holes provided on the conical surface of the upper gas distributor (4) of the gasifier, and the aperture ratio is 1% - 5%.

4. The method according to claim 1 or 2, characterized in that, The raw material inlet (2) is located between 1 / 5 and 3 / 5 of the height of the upper space. And / or, the return material outlet (7) of the gasifier is located between 1 / 5 and 4 / 5 of the height of the lower layer space; And / or, the return material inlet (19) of the gasifier is located between 1 / 3 and 2 / 3 of the height of the upper layer space.

5. The method according to claim 1 or 2, characterized in that, The return material inlet (9) of the regenerator is located below the regenerator (10), and the position is lower than 1 / 2 of the height of the regenerator (10); And / or, the regenerator (10) is provided with 1 to 5 carrier feeding ports (11), and the carrier feeding ports (11) are located in the middle of the regenerator (10).

6. The method according to claim 5, wherein The return material inlet (9) of the regenerator is located between 1 / 5 and 1 / 2 of the height of the regenerator (10); And / or, the carrier feeding port (11) is located between 1 / 3 and 2 / 3 of the height of the regenerator (10).

7. The method according to claim 1 or 2, characterized in that, The reaction temperature in the fluidized bed gasifier (1) is 600 - 900 °C, and the gas phase linear velocity is 0.1 - 1.0 m / s; the reaction temperature in the regenerator (10) is 800 - 1200 °C, and the gas phase linear velocity is 1 - 10 m / s; the reaction pressure ranges in both the fluidized bed gasifier (1) and the regenerator (10) are 0 - 2.0 MPa.

8. The method according to claim 1 or 2, characterized in that The molar ratio of water vapor to carbon in the raw coal, i.e., the water - carbon ratio, is 1.0 - 5.0 mol / mol.

9. The method according to claim 1 or 2, characterized in that, The oxygen - containing gas introduced into the regenerator gas distributor (12) is selected from one or more of oxygen, air, and oxygen - enriched air; And / or, the molar ratio of oxygen to carbon in the oxygen - containing gas, i.e., the oxygen - carbon ratio, is greater than or equal to 1.5 mol / mol.

10. The method according to claim 1 or 2, characterized in that, The heat carrier is selected from natural ores; or a mixture of alkali metals, transition metals and natural ores, or a mixture of alkali metals, transition metals and alkaline earth metal Ca.

11. The method according to claim 10, wherein The natural ore is limestone, dolomite or olivine; And / or, the alkali metal, transition metal or alkaline earth metal Ca is loaded on the carriers of Al2O3, ZrO2, TiO2 or SiO2 by impregnation method, dry - mixing method or ion - exchange method according to 0.1 - 30% of the active component accounting for the weight of the catalyst.

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