A system for producing low-tar and low-methane content syngas from biomass gasification

Abstract

The utility model provides a biomass gasification system for producing low-tar and low-methane content synthesis gas, comprising a gasification system, a high-temperature converter system, a synthesis gas quenching system, a high-temperature dust removal system, a waste heat recovery system, a synthesis gas washing system and a synthesis gas circulation system; the gasification system comprises a biomass pressurized feeding system, a gasification furnace system and a pressurized slag removal system, the biomass pressurized feeding system is used for biomass feeding and pressurization, the gasification furnace system is used for gasifying biomass and generating synthesis gas, the utility model has the beneficial effects of pressurized pure oxygen gasification, reducing the content of impurity gases in the synthesis gas, increasing the pressure of the synthesis gas, reducing the load of the purification system and the power consumption of synthesis compression, and significantly reducing the overall energy consumption.

Description

Technical Field

[0001] The utility model relates to the technical field of biomass gasification to produce synthesis gas, in particular to a biomass gasification to produce low-tar and low-methane content synthesis gas system. Background Art

[0002] As a renewable resource, biomass has the characteristics of abundant resource output, wide geographical distribution and stable energy reserves. The utilization of biomass at home and abroad mainly adopts thermal conversion methods such as direct combustion, pyrolysis and gasification. However, due to the characteristics of high volatile matter and high alkali metal content of biomass, problems such as coking, high alkali metal fly ash contamination and difficult tar treatment often occur during the utilization process. Experiments and practice have proved that the tar produced by biomass gasification changes from gas to liquid when the temperature is lower than 300°C. The liquid tar has high viscosity and adheres to the heating surface, causing the heat exchange surface to quickly contaminate and coke, affecting the normal operation of the equipment. Due to the high alkali metal content in fly ash, the condensation of potassium and sodium can easily cause dust accumulation in the system's waste heat recovery system. The methane content of biomass gasification synthesis gas is high, and the volume fraction can reach more than 10%, resulting in a large amount of venting gas in the subsequent synthesis system, causing great waste. In addition, since the synthesis usually requires highly purified CO+H2 and is carried out under high pressure, the synthesis gas produced by atmospheric pressure air gasification has a high nitrogen content, which increases the burden on the purification system, and the synthesis gas needs to be compressed, which greatly increases the energy consumption of the system. Pure oxygen pressurized gasification can effectively reduce the energy consumption of the system. The above problems are all engineering design problems and process system optimization problems, which require creative optimization design to solve.

[0003] Therefore, there is an urgent need for a system and method for producing low-tar and low-methane synthesis gas by biomass gasification to solve the difficulties in this technical field. Utility Model Content

[0004] In order to overcome the above problems existing in the prior art, the utility model provides a system for producing low-tar and low-methane content synthesis gas by biomass gasification.

[0005] The utility model discloses a system for preparing low-tar and low-methane content synthesis gas by biomass gasification, comprising a gasification system, a high-temperature converter system, a synthesis gas quenching system, a high-temperature dust removal system, a waste heat recovery system, a synthesis gas washing system and a synthesis gas circulation system; the gasification system comprises a biomass pressurized feeding system, a gasification furnace system and a pressurized slag removal system, the biomass pressurized feeding system is used for biomass feeding and pressurization, the gasification furnace system is used for gasifying biomass and generating synthesis gas, the high-temperature converter system is used for decomposing tar in the synthesis gas, the synthesis gas quenching system is used for quenching the high-temperature synthesis gas, the high-temperature dust removal system is used for removing fly ash in the synthesis gas, the waste heat recovery system is used for cooling the synthesis gas, and the synthesis gas washing system is used for preliminarily purifying the synthesis gas.

[0006] On this basis, the biomass pressurized feeding system is connected to the feed port of the gasifier system, the slag discharge port of the gasifier system is connected to the pressurized slag discharge system, a bottom slag outlet is arranged below the pressurized slag discharge system, the synthesis gas outlet of the gasifier system is connected to the synthesis gas inlet of the high-temperature converter system, the synthesis gas outlet of the high-temperature converter system is connected to the synthesis gas inlet of the synthesis gas quenching system, the synthesis gas outlet of the synthesis gas quenching system is connected to the synthesis gas inlet of the high-temperature dust removal system, the synthesis gas outlet of the high-temperature dust removal system is connected to the synthesis gas inlet of the waste heat recovery system, the synthesis gas outlet of the waste heat recovery system is connected to the synthesis gas inlet of the synthesis gas washing system, and a fly ash outlet is arranged below the high-temperature dust removal system.

[0007] On this basis, the gasifier system is connected to a gasifying agent.

[0008] On this basis, at least one waste heat recovery system is provided.

[0009] On this basis, the high temperature reformer system is provided with a reformer burner, and the reformer burner is connected with fuel and oxidant.

[0010] On this basis, the synthesis gas outlet of the synthesis gas washing system is divided into two routes, one is for preliminary purification of the synthesis gas and the other is connected to the synthesis gas inlet of the synthesis gas circulation system, the synthesis gas outlet of the synthesis gas circulation system is connected to the synthesis gas inlet of the synthesis gas quenching system, and the other is used as a preliminary purification synthesis gas delivery system, and the synthesis gas circulation system is connected to the high-temperature converter system.

[0011] On this basis, the gasification pressure of the gasification system is 50kPa(g)~2MPa(g), and the gasification temperature is 700℃~900℃.

[0012] On this basis, the gasifying agent is any one or more mixtures of pure oxygen / oxygen-enriched air and steam / CO2.

[0013] On this basis, the gasifier of the gasifier system is one of a fluidized bed, a circulating fluidized bed, and a fixed bed gasifier.

[0014] A method for producing low-tar and low-methane content synthesis gas by biomass gasification comprises the following steps:

[0015] Step 1: The biomass enters the biomass pressurized feeding system and then enters the gasifier system;

[0016] Step 2: The synthesis gas generated by the gasification furnace system is dedusted by a cyclone separator to form a crude synthesis gas, and the bottom slag is pressurized and discharged by a pressurized slag discharge system;

[0017] Step 3: The crude synthesis gas is sent to the high-temperature reformer and mixed with the high-temperature gas produced by the reformer burner. The temperature is raised to 1000℃~1100℃, and the tar and methane in the crude synthesis gas are converted at high temperature.

[0018] Step 4: chilling the reformed synthesis gas at the outlet of the reformer to a temperature of 500° C. to 600° C. to form chilled synthesis gas;

[0019] Step 5: The quenched synthesis gas is dedusted by a high-temperature dust collector to form a dust-removed synthesis gas, which enters the waste heat recovery system;

[0020] Step six: The waste heat recovery synthesis gas enters the washing system. The synthesis gas outlet of the washing system is divided into two routes. One route is connected to the synthesis gas inlet of the synthesis gas circulation system. A part of the low-temperature preliminary purified synthesis gas 2 after the washing system is taken, and the converted synthesis gas of step 4 is quenched after being pressurized by the circulating gas compressor. The other route is used as the preliminary purified synthesis gas 1 to be sent out of the system.

[0021] Compared with the prior art, the beneficial effects of the utility model are:

[0022] (1) The utility model adopts pressurized pure oxygen gasification, which reduces the content of impurity gases in the synthesis gas, increases the pressure of the synthesis gas, reduces the load of the purification system and the power consumption of synthesis compression, and significantly reduces the overall energy consumption;

[0023] (2) The utility model adopts a high-temperature converter to further convert the synthesis gas produced by the gasification furnace, and converts the tar and methane in the synthesis gas at high temperature; the high-temperature heat source comes from the off-gas of chemical synthesis, and no additional energy is added; the off-gas and oxygen / steam are burned in the burner chamber, and the heat generated heats the synthesis gas, and the oxygen does not react with the synthesis gas, thereby avoiding the loss of effective gas. The existing synthesis gas tar purification generally adopts a water washing method, which will produce a large amount of tar-containing wastewater.

[0024] (3) The utility model adopts the circulating quenching of low-temperature synthesis gas after washing and purification, and quenches the high-temperature conversion gas to below 700°C, so as to facilitate the stable operation of the high-temperature dust removal equipment, and solidify the alkali metal at the same time to avoid the alkali metal contamination of the waste heat recovery boiler; through high-temperature dust removal, most of the fly ash is removed, so that relatively clean synthesis gas enters the waste heat boiler, which greatly optimizes the working conditions of the high-temperature side of the waste heat boiler, avoids boiler ash accumulation, wear, corrosion, etc., and solves the existing synthesis cooling scheme that mostly adopts water quenching or direct waste heat recovery boiler cooling, which will cause heat waste or waste heat recovery boiler contamination and slagging. BRIEF DESCRIPTION OF THE DRAWINGS

[0025] Figure 1 This is a schematic diagram of the structure of the first embodiment of the utility model;

[0026] Figure 2 It is a structural schematic diagram of the second embodiment of the utility model.

[0027] In the figure: 1. biomass, 2. biomass pressurized feeding system, 3. gasifying agent, 4. gasifier system, 5. pressurized slag discharge system, 6. bottom ash, 7. oxidant, 8. fuel, 9. converter burner, 10. high-temperature converter system, 11. synthesis gas quenching system, 12. high-temperature dust removal system, 13. waste heat recovery system, 14. washing system, 15. synthesis gas circulation system, 16. preliminary purification of synthesis gas 1, 17. fly ash, 18. crude synthesis gas, 19. conversion synthesis gas, 20. quenching synthesis gas, 21. dust removal synthesis gas, 22. waste heat recovery synthesis gas, 23. preliminary purification of synthesis gas 2, 24. circulating synthesis gas. DETAILED DESCRIPTION

[0028] The present invention is further described in detail below in conjunction with the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are only used to explain the present invention and are not used to limit the present invention.

[0029] The utility model discloses a biomass gasification system for producing low-tar and low-methane content synthesis gas. Biomass 1 generally refers to shaped biomass fuel after granulation or briquetting. Biomass 1 enters biomass pressurized feeding system 2. Biomass pressurized feeding system 2 generally refers to a pressurized pneumatic conveying system, which is composed of a lock bucket, a generator tank and a discharger. The pressure source is pressurized CO2 gas, nitrogen and other gases. In this embodiment, pressurized CO2 gas is selected. In addition to the pneumatic conveying method, pressurized feeding can also be achieved through a screw feeder with a gas seal. In order to improve the reliability of the feeding system, the feeding equipment is usually set as a standby.

[0030] The biomass pressurized feeding system 2 is connected to the feeding port of the gasification furnace system 4. The gasification furnace system 4 includes a gasification furnace, a cyclone separator, a slag discharge pipe, and a gasification agent preheating device. The gasification furnace is one of a fluidized bed, a circulating fluidized bed, and a fixed bed gasification furnace. In this embodiment, a circulating fluidized bed gasification furnace is selected. The gasification agent 3 is added to the gasification furnace system 4. The gasification agent 3 is any one or more mixtures of pure oxygen / oxygen-enriched air and steam / CO2. In this embodiment, it is a combination of pure oxygen and steam. After being preheated, it enters the gasification furnace. The gasification system The system gasification pressure is 50kPa(g)~2MPa(g), and the gasification temperature is 700℃~900℃. In this embodiment, the gasification pressure is 150kPa(g)~1.2MPa(g), and the gasification temperature is 750℃~850℃. The generated synthesis gas is formed into a crude synthesis gas 18 after dust removal by a cyclone separator. The particles captured by the cyclone separator are returned to the gasifier for reaction. The slag discharge port of the gasifier system 4 is connected to the pressurized slag discharge system 5, and the bottom slag 6 is discharged after being pressurized by the pressurized slag discharge system 5.

[0031] The synthesis gas outlet of the gasifier system 4 is connected to the synthesis gas inlet of the high-temperature converter system 10. The crude synthesis gas 18 generated by the gasifier system 4 enters the high-temperature converter system 10. The conversion temperature of the high-temperature converter system 10 is 950-1200°C. The heat source comes from the converter burner 9. The fuel of the converter burner 9 is synthesis purge gas, waste gas with calorific value, methane, diesel and other fuels. In this embodiment, synthesis purge gas is selected, and the crude synthesis gas 18 is mixed with the high-temperature gas generated by the converter burner 9. The temperature is raised to 1000°C-1100°C. The tar and methane in the crude synthesis gas 18 are converted at high temperature, and their content is greatly reduced.

[0032] The reformer burner 9 is connected to the fuel 8 and the oxidant 7. The principle of selecting the fuel 8 is to utilize the waste gas as much as possible without adding impurity gas. Usually, the purge gas of the subsequent synthesis process is selected. In the application scenario of biomass gasification and hydrogen production, natural gas, diesel and other fuels can be selected. By adding a certain amount of oxidant 7, the flame temperature of the reformer burner 9 is reduced. In this embodiment, steam is selected. Adding steam is also beneficial to the conversion of tar and methane.

[0033] The high-temperature synthesis gas coming out of the high-temperature reformer system 10 is at a high temperature and cannot be directly subjected to deep dust removal. Therefore, a synthesis gas quenching system 11 is provided. The outlet of the synthesis gas quenching system 11 is low-temperature gas, which is combined with the high-temperature gas at the outlet of the reformer 10 and enters the synthesis gas quenching system 11. The high-temperature gas is cooled down. The synthesis gas outlet of the synthesis gas circulation system 15 is connected to the synthesis gas inlet of the synthesis gas quenching system 11. The quenching medium is the low-temperature circulating synthesis gas 24. The low-temperature circulating synthesis gas 24 is a pressurized low-temperature gas with a temperature of about 40°C. After the low-temperature circulating synthesis gas 24 is combined with the high-temperature synthesis gas 19, the temperature of the high-temperature synthesis gas 19 will be reduced. The temperature of the low-temperature circulating synthesis gas 24 entering the synthesis gas quenching system 11 is 40°C to 18 0℃, in this embodiment, the temperature is 40-120℃, the temperature of the quenched synthesis gas 20 at the outlet of the synthesis gas quenching system 11 is 500-750℃, in this embodiment, the temperature is 500-600℃, the synthesis gas outlet of the synthesis gas circulation system 15 is connected to the synthesis gas inlet of the synthesis gas quenching system 11, and the synthesis gas outlet of the high-temperature converter system 10 is connected to the synthesis gas inlet of the synthesis gas quenching system 11. A part of the low-temperature gas after the washing tower 14 is taken and pressurized by the circulating gas compressor 15 to quench the converted synthesis gas 19 at the outlet of the converter 10 to form the quenched synthesis gas 20, and the temperature is quenched to 500℃-600℃. At this temperature, a ceramic filter or a metal sintered filter can be selected to remove dust from the synthesis gas.

[0034] The syngas outlet of the syngas quenching system 11 is connected to the syngas inlet of the high-temperature dust removal system 12. The high-temperature dust removal system 12 is a high-temperature and pressure-resistant dust collector. The dust-removed syngas 21 at the dust collector outlet quenches the syngas 20 and forms the dust-removed syngas 21 after dust removal by the high-temperature dust collector 12. The dust content of the dust-removed syngas 21 is less than 100 mg / Nm3, and in this embodiment, it is less than 30 mg / Nm3. The temperature is about 500°C to 600°C, and enters the waste heat recovery system 13. At this dust content and temperature, the impact of the fly ash in the dust-removed syngas 21 on the waste boiler has been reduced to a very low level. The synthesis gas outlet of the high-temperature dust removal system 12 is connected to the synthesis gas inlet of the waste heat recovery system 13. The waste heat recovery system 13 is a waste heat boiler, which can be a water tube boiler or a fire tube boiler. The waste heat recovery system 13 includes an evaporator, a superheater, an economizer, a steam drum, a circulating pump and other equipment. In this embodiment, the heat of the dust removal synthesis gas 21 is recovered by the waste heat boiler to generate superheated steam. The temperature of the superheated steam is 200°C~300°C; the temperature of the waste heat recovery synthesis gas 22 after recovering the heat is 160°C~180°C.

[0035] The steam produced by the waste heat recovery system 13 is superheated steam, and the temperature of the superheated steam is 180°C~400°C, and in this embodiment, it is 200°C~300°C; the temperature of the initial outlet synthesis gas 22 of the waste heat recovery system 13 is 140°C~220°C, and in this embodiment, it is 160°C~180°C.

[0036] The syngas outlet of the waste heat recovery system 13 is connected to the syngas inlet of the syngas washing system 14, and the waste heat recovery syngas 22 enters the washing system 14. The washing system 14 usually includes a venturi scrubber, a washing tower, a washing water cooler, and a washing water circulation pump. The syngas outlet of the syngas washing system 14 is divided into two routes, one of which is connected to the syngas inlet of the syngas circulation system 15, and the other is used as a preliminary purified syngas 16 delivery system. The syngas circulation system 15 is connected to the high-temperature reformer system 10. The temperature of the preliminary purified syngas 23 after washing is preferably 40°C to 120°C. The temperature of the syngas after washing is affected by the circulation amount of the quenching gas and the system pressure. The washing temperature should be selected to minimize the amount of the quenching circulation syngas to reduce energy consumption.

[0037] Example 2

[0038] The difference from Example 1 is that the system is equipped with two waste heat recovery systems 13. The quenched synthesis gas 20 first enters the waste heat boiler 1 31. The synthesis gas 30 after the temperature is reduced to 300°C~400°C enters the high-temperature dust collector 12, and the dust-removed synthesis gas 21 enters the waste heat boiler 2 13. The purpose of setting the waste heat boiler 31 is to appropriately reduce the temperature of the synthesis gas entering the high-temperature dust collector, so that the selection of the high-temperature dust collector is more flexible.

[0039] This application realizes the production of low-tar and low-methane synthesis gas by pure oxygen pressurized gasification of biomass through innovative system design and reasonable process parameter setting, solves the engineering problems of tar, alkali metals, etc. in biomass gasification to produce synthesis gas, and improves the reliability of the system.

[0040] Example 3

[0041] A method for producing low-tar and low-methane content synthesis gas by biomass gasification comprises the following steps:

[0042] Step 1: biomass 1 enters biomass pressurized feeding system 2 and is pressurized before entering gasification furnace system 4;

[0043] Step 2: The synthesis gas generated by the gasification furnace system 4 is dedusted by the cyclone separator to form a crude synthesis gas 18, and the bottom slag 6 is pressurized and discharged by the pressurized slag discharge system 5;

[0044] Step 3: The crude synthesis gas 18 is fed into the high-temperature reformer system 10, mixed with the high-temperature gas generated by the reformer burner 9, and the temperature is raised to 1000°C to 1100°C, and the tar and methane in the crude synthesis gas 18 are converted at high temperature;

[0045] Step 4: Take a portion of the low-temperature preliminary purified synthesis gas 23 after the washing system 14, and pressurize it through the circulating gas compressor 15 to quench the reformed synthesis gas 19 at the outlet of the reformer 10. The low-temperature circulating synthesis gas 24 is a pressurized low-temperature gas with a temperature of about 40°C. After the low-temperature circulating synthesis gas 24 is combined with the high-temperature synthesis gas 19, the temperature of the high-temperature synthesis gas 19 will be reduced, and the temperature is quenched to 500°C to 600°C to form a quenched synthesis gas 20;

[0046] Step 5: The quenched synthesis gas 20 is dedusted by the high temperature dust collector 12 to form the dedusted synthesis gas 21, which enters the waste heat recovery system 13;

[0047] Step six: The waste heat recovery synthesis gas 22 enters the washing system 14. The synthesis gas outlet of the washing system 14 is divided into two paths. One path is the preliminary purified synthesis gas 2 23 connected to the synthesis gas inlet of the synthesis gas circulation system 15, that is, to quench the converted synthesis gas 19 in step four, and the other path is used as the preliminary purified synthesis gas 16 to be sent out of the system.

[0048] In the description of the present invention, it should be understood that the terms "coaxial", "bottom", "one end", "top", "middle", "the other end", "upper", "one side", "top", "inside", "front", "center", "both ends" and the like indicate orientations or positional relationships based on the orientations or positional relationships shown in the accompanying drawings, and are only for the convenience of describing the present invention and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and therefore should not be understood as a limitation on the present invention.

[0049] In the present utility model, unless otherwise clearly stipulated and limited, the terms such as "installation", "setting", "connection", "fixation", "screwing", "pad installation" and the like should be understood in a broad sense. For example, it can be a fixed connection, a detachable connection, or an integral one; it can be a mechanical connection or an electrical connection; it can be a direct connection or an indirect connection through an intermediate medium; it can be the internal connection of two elements or the interaction relationship between two elements. Unless otherwise clearly defined, ordinary technicians in this field can understand the specific meanings of the above terms in the utility model according to the specific circumstances.

[0050] The above description shows and describes the preferred embodiments of the utility model. As mentioned above, it should be understood that the utility model is not limited to the form disclosed herein, and should not be regarded as excluding other embodiments, but can be used in various other combinations, modifications and environments, and can be modified within the scope of the utility model concept described herein through the above teachings or the technology or knowledge of the relevant field. The changes and modifications made by those skilled in the art do not depart from the spirit and scope of the utility model, and should be within the scope of protection of the claims attached to the utility model.

Claims

1. A system for producing low-tar and low-methane content synthesis gas by biomass gasification, characterized by: The invention comprises a gasification system, a high-temperature reformer system (10), a synthesis gas quenching system (11), a high-temperature dust removal system (12), a waste heat recovery system (13), a synthesis gas washing system (14) and a synthesis gas circulation system (15); the gasification system comprises a biomass pressurized feeding system (2), a gasification furnace system (4) and a pressurized slag removal system (5), The biomass pressurized feeding system (2) is used for biomass feeding and pressurization. The gasifier system (4) is used to gasify biomass and generate synthesis gas. The high temperature reformer system (10) is used to decompose tar in the synthesis gas. The synthesis gas quenching system (11) is used to quench the high-temperature synthesis gas. The high temperature dust removal system (12) is used to remove fly ash from the synthesis gas. The waste heat recovery system (13) is used to cool the synthesis gas. The synthesis gas washing system (14) is used to preliminarily purify the synthesis gas.

2. The system for producing low-tar and low-methane content synthesis gas by biomass gasification according to claim 1, characterized in that: The biomass pressurized feeding system (2) is connected to the feed port of the gasifier system (4), the slag discharge port of the gasifier system (4) is connected to the pressurized slag discharge system (5), a bottom slag (6) outlet is arranged below the pressurized slag discharge system (5), the synthesis gas outlet of the gasifier system (4) is connected to the synthesis gas inlet of the high-temperature converter system (10), the synthesis gas outlet of the high-temperature converter system (10) is connected to the synthesis gas inlet of the synthesis gas quenching system (11), the synthesis gas outlet of the synthesis gas quenching system (11) is connected to the synthesis gas inlet of the high-temperature dust removal system (12), the synthesis gas outlet of the high-temperature dust removal system (12) is connected to the synthesis gas inlet of the waste heat recovery system (13), the synthesis gas outlet of the waste heat recovery system (13) is connected to the synthesis gas inlet of the synthesis gas washing system (14), and a fly ash (17) outlet is arranged below the high-temperature dust removal system (12).

3. The system for producing low-tar and low-methane content synthesis gas by biomass gasification according to claim 2, characterized in that: The gasification furnace system (4) is connected to a gasifying agent (3).

4. The system for producing low-tar and low-methane content synthesis gas by biomass gasification according to claim 2, characterized in that: At least one waste heat recovery system (13) is provided.

5. The system for producing low-tar and low-methane content synthesis gas by biomass gasification according to claim 2, characterized in that: The synthesis gas outlet of the synthesis gas washing system (14) is divided into two paths, one of which is used for preliminary purification of synthesis gas 2 (23) connected to the synthesis gas inlet of the synthesis gas circulation system (15), and the synthesis gas outlet of the synthesis gas circulation system (15) is connected to the synthesis gas inlet of the synthesis gas quenching system (11), and the other path is used as a preliminary purification of synthesis gas 1 (16) delivery system, and the synthesis gas circulation system (15) is connected to the high-temperature reformer system (10).

6. The system for producing low-tar and low-methane content synthesis gas by biomass gasification according to claim 5, characterized in that: The high-temperature reformer system (10) is provided with a reformer burner (9), and the reformer burner (9) is connected to the fuel (8) and the oxidant (7).

7. The system for producing low-tar and low-methane content synthesis gas by biomass gasification according to claim 1, characterized in that: The gasification pressure of the gasification system is 50 kPa(g) to 2 MPa(g), and the gasification temperature is 700°C to 900°C.

8. The system for producing low-tar and low-methane content synthesis gas by biomass gasification according to claim 3, characterized in that: The gasifying agent (3) is any one or more mixtures of pure oxygen / oxygen-enriched air and steam / CO2.

9. The system for producing low-tar and low-methane content synthesis gas by biomass gasification according to claim 2, characterized in that: The gasifier of the gasifier system (4) is one of a fluidized bed, a circulating fluidized bed, and a fixed bed gasifier.

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