CN109294625B - Fluidized gasification pre-oxidation reactor - Google Patents
Fluidized gasification pre-oxidation reactor Download PDFInfo
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- CN109294625B CN109294625B CN201811032431.0A CN201811032431A CN109294625B CN 109294625 B CN109294625 B CN 109294625B CN 201811032431 A CN201811032431 A CN 201811032431A CN 109294625 B CN109294625 B CN 109294625B
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- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
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Abstract
A fluidized gasification preoxidation reactor relates to a clean energy preoxidation reactor, which is connected with a conveying bed or a riser gasification reactor to form a conveying bed or a downer preoxidation reactor, fuel enters the preoxidation reactor to be dried/pyrolyzed or partially gasified, and products generated by the preoxidation reactor are directly subjected to semicoke gasification and tar deep cracking/reforming in the fluidized gasification reactor to produce low-tar-content synthetic gas or fuel gas. The pre-oxidation reactor of the conveying bed and the downstream bed has strong fuel adaptability, strong gas-solid interaction, reduced pressure and simple and convenient operation. The gasification process of coupling pre-oxidation can almost completely convert tar, effectively reduce the consumption of gasification steam and realize high-efficiency gasification.
Description
Technical Field
The invention relates to a clean energy pre-oxidation reactor, in particular to a fluidized gasification pre-oxidation reactor.
Background
Gasification refers to the conversion of solid fuels into fuels containing CO and H by taking carbonaceous fuels (coal, coal coke or biomass, etc.) as raw materials and taking oxygen (air, oxygen-enriched oxygen or industrial pure oxygen), water vapor or hydrogen as gasifying agents, and carrying out a series of chemical reactions at a certain temperature and pressure in specific equipment2、CH4And waiting for combustible gas. Along with the increasing shortage of natural gas and petroleum resources in the world, gasification is an important technical means for reducing environmental pollution, saving energy and realizing comprehensive clean utilization of carbon-containing fuels. Existing gasification technologies are generally classified into three major groups, fixed bed gasification, fluidized bed gasification and entrained flow gasification. Fixed bed gasification, also called moving bed gasification, is a technology in which coal is gasified by a gasifying agent fed from the bottom of a gasification furnace while being gradually moved downward in a reverse direction to a generated gas, and the sensible heat of the gasified generated gas is effectively utilized, the outlet temperature of the generated gas is low, the carbon content of slag discharged from the bottom of the gasification furnace is low, and fixed bed gasification actually represents the most efficient gasification technology. However, the fixed bed gasification furnace commonly used in China at present generally has the problems of poor raw material applicability, small treatment capacity, difficult amplification, low gas conversion efficiency, high tar content in produced gas and the like, and further amplification and clean use of the gasification technology are severely restricted. The fluidized bed gasification furnace has higher heat transfer and mass transfer rates, can process small-particle-size raw materials, is suitable for large-scale production, and generates stable fuel gas with stable composition and heat value. But the gas generatedStill contains a certain amount of tar and has low calorific value. In addition, carbon conversion is lower due to the higher carbon content in the ash. The entrained flow bed has high gasification reaction temperature, high gasification strength and high carbon conversion rate, is suitable for large coal chemical industry bases, but has poor raw material flexibility and is difficult to be used for treating large-particle biomass and other raw materials.
In view of the problems associated with the production of gas by a single gasification technology, two-stage gasification technology was rapidly becoming a focus of research once it was introduced at the end of the 20 th century. Two-stage gasification technologies can be broadly divided into two categories: the first type combines a gasifier with a high temperature tar reformer, and utilizes the high temperature, partial oxidation, and catalytic action of a catalyst in the reformer to remove tar. The process has the advantages of long flow, low gasification efficiency and difficult industrial amplification, the catalyst is easy to cause carbon deposition in the tar cracking process, the catalyst is quickly inactivated, the conversion rate of the tar is often low, and the regeneration cost of the catalyst is increased. The other method is that the traditional fuel gasification process is divided into two sub-processes of raw material pyrolysis and semicoke gasification based on the decoupling concept and is respectively carried out in two reactors, and the tar is separated by fully utilizing the catalytic action of pyrolysis semicoke. The process flow is short, tar removal is completed while fuel gasification is carried out, the tar content in the gas is low, the purification investment is low, and the cost is favorably reduced.
The two-stage gasification technologies currently in use are fixed bed two-stage gasification and fluidized bed two-stage gasification. The institute of process engineering of the Chinese academy of sciences developed a two-stage gasification process (CN 1916123) coupling a fluidized bed and a downdraft fixed bed, which decouples the gasification process into two sub-processes of pyrolysis and gasification, which are respectively carried out in a fluidized bed pyrolyzer and a downdraft fixed bed gasification furnace. The process combines the advantages of a fluidized bed and a downdraft fixed bed, and can effectively reduce the tar content through the catalytic reforming action of a semicoke bed layer. Because the upper fluidized bed pyrolyzer is suitable for processing raw materials with smaller particle size, when finer particles enter a downdraft fixed bed to carry out gasification reaction, the problems of poor ventilation of the fixed bed and overlarge pressure drop of the whole bed are easily caused, and in addition, the fixed bed reactor also has the defect of difficult industrial amplification, so that the process needs to be further improved and optimized. Chinese patent No. 201210144562.4 relates to a two-stage gasification method for fuel with wide particle size distribution and a gasification device thereof. The traditional fuel gasification process is divided into two sub-processes of raw material pyrolysis and semicoke gasification, and the two sub-processes are respectively carried out in an upstream fluidized bed pyrolyzer and a downstream entrained flow gasifier. However, the fluidized bed gasification furnace in the invention has low operation gas velocity, the reaction is mainly carried out in a dense phase region, the material at the upper part of the reactor is relatively thin, the temperature difference between the dense phase region and the thin phase region is relatively large, the bed material amount is large, the bed pressure drop is relatively large, the operation is not flexible, and the industrial amplification is difficult.
Most of pyrolyzers in the two-stage gasification process are fixed beds and bubbling fluidized beds, which inevitably causes the problems of overlarge bed pressure drop and difficult industrial scale-up.
Disclosure of Invention
The invention aims to provide a fluidized gasification pre-oxidation reactor, which applies a transport bed and a downer pre-oxidation reactor to two-stage gasification. When the pre-oxidation reactor is a conveying bed, the high-temperature particles circularly entering the reactor can heat the cold fuel and the oxygen-containing gas entering the reactor, so that the temperature of the oxygen-containing gas fed into the reactor is increased, the gas velocity is increased, a dense-phase region is reduced, the pressure drop of a bed layer is smaller, and the application of small-particle fuel is facilitated. When the pre-oxidation reactor is a descending bed, the bed layer has no pressure drop and no power consumption, and is favorable for the application of large-particle irregular fuel.
The purpose of the invention is realized by the following technical scheme:
the reactor aims at the gasification process of particle fuel by taking a conveying bed or a lifting pipe as a gasification reactor, the process comprises the steps of connecting a fuel preoxidation reactor with the gasification reactor, adding fuel into the preoxidation reactor, sending gas-solid products formed by pyrolysis and preoxidation into the gasification reactor, and then carrying out gasification reaction and cracking reaction to realize low-tar gasification;
the specific process is as follows:
the fuel is fed to a pre-oxidation reactor and dried/pyrolyzed or partially gasified by heating of high temperature particles recycled to the reactor or oxidation of oxygen-containing gas fed to the reactor. The products generated in the pre-oxidation reactor enter a downstream gasification reactor through a pipeline, meanwhile, oxygen-containing gas is introduced into the bottom of the gasification reactor, the semicoke is gasified in the gasification furnace, meanwhile, the tar is removed by utilizing the high-temperature cracking, partial gasification and catalytic reforming action of the semicoke on the tar in the gasification furnace, the synthetic gas or fuel gas with low tar content is produced, and the unreacted high-temperature particles of the semicoke and the like return to the pre-oxidation reactor after gas-solid separation.
The fuel of the fluidized gasification pre-oxidation reactor comprises granular raw materials suitable for producing synthesis gas/fuel gas by fluidized gasification, such as coal, biomass, semicoke, petroleum coke and the like.
The fluidized gasification pre-oxidation reactor is supplied with oxygen-containing gas, and heat required for pyrolysis and pre-oxidation reaction is provided by combusting combustible materials in the pre-oxidation reactor through the oxygen-containing gas.
The fluidized gasification pre-oxidation reactor is characterized in that high-temperature particles obtained by gas-solid separation after the gasification reactor, including unreacted fuel particles, fuel ash, added bed material particles and the like, are returned to the pre-oxidation reactor to provide heat required for pyrolysis and pre-oxidation reaction.
The fluidized gasification pre-oxidation reactor is in a conveying bed mode, fuel is added into the conveying bed pre-oxidation reactor, and the fuel is dried/pyrolyzed or partially gasified under the action of heating of high-temperature particles circularly entering the reactor or the oxidation of oxygen-containing gas fed into the reactor from the bottom of the conveying bed.
The pre-oxidation reactor is in a conveying bed mode, oxygen-containing gas is supplied from the bottom of the conveying bed pre-oxidation reactor, high-temperature particles are supplied from the side face of the lower part of the conveying bed reactor, fuel is supplied into the pre-oxidation reactor at the side face position above a high-temperature particle supply port, the fuel and the high-temperature particles are mixed and transferred heat in the pneumatic upward conveying process and simultaneously react with the oxygen-containing gas to carry out pyrolysis and pre-oxidation reactions, and generated gas-solid products are sent into the gasification reactor through a discharge port at the top or the upper part of the conveying bed.
The pre-oxidation reactor for fluidized gasification is in a conveying bed mode, and an inlet of high-temperature particles circularly entering the reactor after gas-solid separation is arranged on the side face of the lower part of the conveying bed pre-oxidation reactor.
The fluidized gasification preoxidation reactor is characterized in that the downer mode is that fuel is added into the downer preoxidation reactor, and the fuel is dried/pyrolyzed or partially gasified under the action of heating of high-temperature particles circularly entering the reactor or oxidation of oxygen-containing gas fed into the reactor from the top of the downer.
The pre-oxidation reactor for fluidized gasification is in a descending bed mode, high-temperature particles are fed from the top of the descending bed pre-oxidation reactor, oxygen-containing gas and fuel are fed from the top or the upper half part of the pre-oxidation reactor, the fuel and the high-temperature particles are mixed and transfer heat in the descending process, and simultaneously react with the oxygen-containing gas to carry out pyrolysis and pre-oxidation reactions, and generated gas-solid products are fed into the gasification reactor from the bottom of the descending bed.
The invention has the advantages and effects that:
1. the reactor and the conveying bed or the riser gasification reactor are connected with the conveying bed or the downer preoxidation reactor, fuel enters the preoxidation reactor to be dried/pyrolyzed or partially gasified, and products generated in the preoxidation reactor are directly subjected to semicoke gasification and tar deep cracking/reforming in the fluidized gasification reactor to produce low-tar-content synthetic gas or fuel gas.
2. The pre-oxidation reactor of the conveying bed and the downer has strong fuel adaptability, strong gas-solid interaction, reduced pressure and simple and convenient operation. The gasification process of coupling pre-oxidation can almost completely convert tar, effectively reduce the consumption of gasification steam and realize high-efficiency gasification.
Drawings
FIG. 1 is a block diagram of the operating principle of a fluidized gasification pre-oxidation reactor according to the present invention;
FIG. 2 is a schematic diagram of the two-stage gasification process of a transport bed pre-oxidation reactor of the present invention;
FIG. 3 is a schematic diagram of the two-stage gasification process of a downer pre-oxidation reactor of the present invention.
Detailed Description
The present invention will be described in detail with reference to the embodiments shown in the drawings.
Aiming at the particle fuel gasification process taking a conveying bed or a lifting pipe as a gasification reactor, the fluidized gasification preoxidation reactor is connected with the gasification reactor, fuel is added into the preoxidation reactor, and gas-solid products formed by pyrolysis and preoxidation are sent into the gasification reactor to carry out gasification reaction and cracking reaction, so that low-tar gasification is realized. The pre-oxidation reactor is a conveying bed or a descending bed. An oxygen-containing gas is fed into the pre-oxidation reactor, and the heat required for the pyrolysis and pre-oxidation reactions is provided by combusting combustibles in the pre-oxidation reactor with the oxygen-containing gas. High-temperature particles obtained by gas-solid separation after the gasification reactor, including unreacted fuel particles, fuel ash, added bed material particles and the like, are returned to the pre-oxidation reactor to provide heat required for pyrolysis and pre-oxidation reaction. The pre-oxidation reactor is a descending bed, the high-temperature particles are fed from the top of the descending bed pre-oxidation reactor, the oxygen-containing gas and the fuel are fed from the top or the upper half part of the pre-oxidation reactor, the fuel and the high-temperature particles are mixed and transferred heat in the descending process and simultaneously react with the oxygen-containing gas to carry out pyrolysis and pre-oxidation reactions, and the generated gas-solid products are fed into the gasification reactor from the bottom of the descending bed. The pre-oxidation reactor is a conveying bed, oxygen-containing gas is supplied from the bottom of the conveying bed pre-oxidation reactor, high-temperature particles are supplied from the side surface of the lower part of the conveying bed reactor, fuel is fed into the pre-oxidation reactor at the side position above a high-temperature particle supply port, the fuel and the high-temperature particles are mixed and transferred heat in the pneumatic upward conveying process and simultaneously react with the oxygen-containing gas to carry out pyrolysis and pre-oxidation reactions, and the generated gas-solid product is fed into the gasification reactor through a discharge port at the top or the upper part of the conveying bed. The fuel includes all particle raw materials suitable for producing synthesis gas/fuel gas by fluidized gasification, such as coal, biomass, semicoke, petroleum coke and the like.
Example 1
As shown in fig. 2, the fuel is fed into a transport bed pre-oxidation reactor and dried/pyrolyzed or partially gasified by heating of high temperature particles recycled into the reactor or by oxidation of an oxygen-containing gas fed into the reactor from the bottom of the transport bed. The products generated in the pre-oxidation reactor enter a downstream gasification furnace through a pipeline, meanwhile, oxygen-containing gas is introduced into the bottom of the gasification furnace, the semicoke is gasified in the gasification furnace, meanwhile, the tar is removed by utilizing the high-temperature cracking, partial gasification and catalytic reforming action of the semicoke on the tar in the gasification furnace, the synthetic gas or fuel gas with low tar content is produced, and the unreacted semicoke returns to the conveying bed pre-oxidation reactor after gas-solid separation.
The oxygen-containing gas is fed from the bottom of the conveying bed preoxidation reactor, the high-temperature particles are fed from the side surface of the lower portion of the conveying bed reactor, the fuel is fed into the preoxidation reactor from the side surface position above the feeding port of the high-temperature particles, the fuel and the high-temperature particles are mixed and transferred in the upward pneumatic conveying process, and simultaneously, the fuel and the high-temperature particles are reacted with the oxygen-containing gas to carry out pyrolysis and preoxidation reaction, and the generated gas-solid product is fed into the gasification reactor through the discharging. The inlet of high-temperature particles circularly entering the reactor after gas-solid separation is arranged on the side surface of the lower part of the conveying bed pre-oxidation reactor.
Example 2
As shown in fig. 3, the fuel is fed into the downer pre-oxidation reactor and is dried/pyrolyzed or partially gasified by heating of the high temperature particles circulated into the reactor or by oxidation of the oxygen-containing gas fed into the reactor from the top of the downer. The generated pyrolysis product enters a downstream gasification furnace through a pipeline, meanwhile, aerobic gas is introduced into the bottom of the gasification furnace, the semicoke is gasified in the gasification furnace, meanwhile, the tar is deeply removed by utilizing the high-temperature cracking, partial gasification and the catalytic reforming action of the semicoke on the tar in the gasification furnace, the synthetic gas or fuel gas with low tar content is produced, and the unreacted semicoke returns to a descending bed pre-oxidation reactor after gas-solid separation.
The high-temperature particles are fed from the top of the downer preoxidation reactor, the oxygen-containing gas and the fuel are fed from the top or the upper half part of the preoxidation reactor, the fuel and the high-temperature particles are mixed and transferred heat in the downer process, and simultaneously react with the oxygen-containing gas to carry out pyrolysis and preoxidation reaction, and the generated gas-solid products are fed from the bottom of the downer to the gasification reactor.
Claims (4)
1. The fluidized gasification preoxidation reactor is characterized in that the reactor aims at the gasification process of granular fuel by taking a conveying bed or a lifting pipe as a gasification reactor, the process comprises the steps of connecting a fuel preoxidation reactor with the gasification reactor, adding the fuel into the preoxidation reactor, sending gas-solid products formed by pyrolysis and preoxidation into the gasification reactor, and then carrying out gasification reaction and cracking reaction to realize low-tar gasification;
the specific process is as follows:
the fuel is fed into a pre-oxidation reactor and dried/pyrolyzed or partially gasified by heating the high-temperature particles circulated into the reactor or oxidizing the oxygen-containing gas fed into the reactor
Products generated in the pre-oxidation reactor enter a downstream gasification reactor through a pipeline, meanwhile, oxygen-containing gas is introduced into the bottom of the gasification reactor, the semicoke is gasified in the gasification furnace, meanwhile, the tar is removed by utilizing the high-temperature cracking, partial gasification and catalytic reforming action of the semicoke on the tar in the gasification furnace, the synthetic gas or fuel gas with low tar content is produced, and unreacted high-temperature particles such as the semicoke and the like return to the pre-oxidation reactor after gas-solid separation;
the pre-oxidation reactor is in a conveying bed mode, oxygen-containing gas is fed from the bottom of the conveying bed pre-oxidation reactor, high-temperature particles are fed from the side face of the lower part of the conveying bed reactor, fuel is fed into the pre-oxidation reactor at the side face position above a high-temperature particle feeding port, the fuel and the high-temperature particles are mixed and transferred heat in the pneumatic upward conveying process and simultaneously react with the oxygen-containing gas to carry out pyrolysis and pre-oxidation reaction, and generated gas-solid products are fed into the gasification reactor through a discharge port at the top or the upper part of the conveying bed;
the pre-oxidation reactor is in a conveying bed mode, and an inlet of high-temperature particles circularly entering the reactor after gas-solid separation is arranged on the side face of the lower part of the conveying bed pre-oxidation reactor;
the pre-oxidation reactor is in a descending bed mode, high-temperature particles are fed from the top of the descending bed pre-oxidation reactor, oxygen-containing gas and fuel are fed from the top or the upper half part of the pre-oxidation reactor, the fuel and the high-temperature particles are mixed and transfer heat in the descending process and simultaneously react with the oxygen-containing gas to generate pyrolysis and pre-oxidation reactions, and generated gas-solid products are fed into the gasification reactor from the bottom of the descending bed.
2. The fluidized gasification pre-oxidation reactor of claim 1, wherein the fuel comprises a particulate feedstock suitable for fluidized gasification to syngas/gas.
3. A fluidized gasification pre-oxidation reactor according to claim 1, wherein oxygen-containing gas is fed into the pre-oxidation reactor, and the heat required for pyrolysis and pre-oxidation reactions is provided by combusting combustibles in the pre-oxidation reactor with the oxygen-containing gas.
4. A fluidized gasification pre-oxidation reactor as claimed in claim 1, wherein high temperature particles obtained by gas-solid separation after the gasification reactor, including unreacted fuel particles, fuel ash and added bed material particles, are returned to the pre-oxidation reactor to provide the heat required for pyrolysis and pre-oxidation reaction.
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| CN115353917B (en) * | 2022-09-14 | 2024-02-20 | 陕西延长石油（集团）有限责任公司 | Annular fluidization viscosity breaking conveying device and method for pulverized coal |
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| CN101781583A (en) * | 2009-01-21 | 2010-07-21 | 中国科学院过程工程研究所 | Method and device for utilizing high value through pyrolysis and gasification of coal |
| CN102703131A (en) * | 2012-05-10 | 2012-10-03 | 中国科学院过程工程研究所 | Two-stage gasification method and gasification device for fuels with wide size distribution |
| CN106995728A (en) * | 2017-05-04 | 2017-08-01 | 中钢集团鞍山热能研究院有限公司 | A kind of fine coal high-efficiency cleaning prepares the process integration of oil gas product |
| CN107502388A (en) * | 2017-09-11 | 2017-12-22 | 哈尔滨工业大学 | Two sections of low temperature gasification device and methods based on low order fuel autocatalysis |
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| CN101781583A (en) * | 2009-01-21 | 2010-07-21 | 中国科学院过程工程研究所 | Method and device for utilizing high value through pyrolysis and gasification of coal |
| CN102703131A (en) * | 2012-05-10 | 2012-10-03 | 中国科学院过程工程研究所 | Two-stage gasification method and gasification device for fuels with wide size distribution |
| CN106995728A (en) * | 2017-05-04 | 2017-08-01 | 中钢集团鞍山热能研究院有限公司 | A kind of fine coal high-efficiency cleaning prepares the process integration of oil gas product |
| CN107502388A (en) * | 2017-09-11 | 2017-12-22 | 哈尔滨工业大学 | Two sections of low temperature gasification device and methods based on low order fuel autocatalysis |
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