CN107760384A - The devices and methods therefor of efficient catalytic coal gasifaction methane rich synthesis gas - Google Patents
The devices and methods therefor of efficient catalytic coal gasifaction methane rich synthesis gas Download PDFInfo
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- CN107760384A CN107760384A CN201610707698.XA CN201610707698A CN107760384A CN 107760384 A CN107760384 A CN 107760384A CN 201610707698 A CN201610707698 A CN 201610707698A CN 107760384 A CN107760384 A CN 107760384A
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- C—CHEMISTRY; METALLURGY
- 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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- C—CHEMISTRY; METALLURGY
- 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
- C10J3/56—Apparatus; Plants
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- C—CHEMISTRY; METALLURGY
- 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
- C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
-
- C—CHEMISTRY; METALLURGY
- 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
- C10J3/72—Other features
- C10J3/82—Gas withdrawal means
- C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
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- C—CHEMISTRY; METALLURGY
- 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
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/093—Coal
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- C—CHEMISTRY; METALLURGY
- 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
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0983—Additives
- C10J2300/0986—Catalysts
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- C—CHEMISTRY; METALLURGY
- 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
- C10J2300/00—Details of gasification processes
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
- C10J2300/164—Integration of gasification processes with another plant or parts within the plant with conversion of synthesis gas
- C10J2300/1656—Conversion of synthesis gas to chemicals
- C10J2300/1662—Conversion of synthesis gas to chemicals to methane (SNG)
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- C—CHEMISTRY; METALLURGY
- 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
- C10J2300/00—Details of gasification processes
- C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
- C10J2300/1807—Recycle loops, e.g. gas, solids, heating medium, water
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
Abstract
The present invention relates to a kind of devices and methods therefor of efficient catalytic coal gasifaction methane rich synthesis gas, solves the problems, such as efficiency of carbon con version present in prior art and gasification low intensity, methane production is relatively low, energy consumption is higher and gasifier operation stability difference.The present invention is made up of fluidized-bed gasification furnace and fluidized bed pyrolysis methanation furnace, it is characterized in that material inlet is located at the top of fluidized bed pyrolysis methanation furnace, the bottom of fluidized bed pyrolysis methanation furnace is connected with fluidized gasification furnace bottom, and the synthesis airway of outlet connection stretches to the bottom of pyrolysis methanation furnace above fluidized-bed gasification furnace.Mainly include the following steps that：The coal sample and high-temperature synthesis gas of supported catalyst carry out being catalyzed pyrolysis and methanation reaction in fluidized bed pyrolysis methanation furnace, semicoke particle and coal ash particle after pyrolysis enter in fluidized-bed gasification furnace the technical scheme for carrying out combustion gasification reaction, preferably solve above mentioned problem, can be applied to coal methane rich synthesis gas field.
Description
Technical field
The present invention relates to a kind of device and method of efficient catalytic coal gasifaction, more specifically, a kind of point of present invention design
The combined catalytic gasification reaction unit of the fluidized bed pyrolysis methanation furnace and fluidized-bed gasification furnace of order reaction and method, belong to coal
Catalytic gasification field.
Background technology
Rich coal, oil-poor, few gas are the energy resource structure features in China, are walked with the fast development and urbanization of China's economy
The quickening cut down, the demand of natural gas is increasingly increased.The gas production in China itself to be unable to reach the demand of natural gas,
Imbalance between supply and demand becomes increasingly conspicuous, and supply breach has dependence import only and made up, and largely have impact on the energy security in China.
In view of China is a coal big country, coal production enriches, and converts coal into natural gas, and it is important to be that Coal Clean efficiently utilizes
Approach, because its energy transformation ratio is high, it is adapted to China's national situation, effectively alleviates the imbalance between supply and demand of natural gas, turn into current coal chemical industry
The important directions of the research field in field.
Conventional natural gas from coal technology is that coal first is converted into synthesis gas (CO+H at this stage2), then carry out methanation and obtain
To SNG method, it is necessary to undergo following steps：Gasification, conversion cooling, purification, methane synthesis etc., i.e. two-step method coal day
The process of right gas.This method energy consumption of reaction is big, heat loss is more, it is necessary to which multiple reaction units thus cause technique also more multiple
It is miscellaneous.However, one-step method natural gas from coal technology is using coal as raw material, the direct synthesizing methane in the presence of catalyst, by
Catalytic gasification, catalytic shift and catalytic production of methane is carried out in same reaction to react to obtain the synthesis gas rich in methane, technology tool
There are higher economy and feasibility, turn into the important research direction in natural gas from coal field.
The patent US4318712 of Exxon companies of the U.S. discloses a kind of technological process of coal one-step method methane directly processed, will
Coal and catalyst are mixed in laggard fluidized bed gasification furnace, are passed through 850 DEG C of high temperature super heated steam, maintain the reaction temperature in stove
At 700 DEG C or so, reaction pressure 3.5MPa, gasified simultaneously in the effect of catalyst, changed and methanation reaction, gasification furnace
The synthesis gas of outlet isolates methane by the method for cryogenic separation, and by isolated CO+H2As circulation synthesis gas with
High-temperature vapour mixes, and is passed through fluidized-bed gasification furnace forced mathane course of reaction again.The process adds the deep cooling of complexity point
From unit, and circulate being passed through for synthesis gas and reduce gasification rate and efficiency of carbon con version.
The patent US20070000177A1 of GPE companies of the U.S. proposes a kind of more advanced on the basis of Exxon technologies
Coal one-step method methane technique, using alkali carbonate or the effective catalyst of alkali metal hydroxide, and add
Calcium oxide is used for caused carbon dioxide during absorbing reaction, so as to directly obtaining methane-rich gas.But GPE techniques with
Exxon techniques are identical, are required to superheated steam being heated to 850 DEG C or so, and energy consumption is higher, and the residence time of coal particle is longer,
Efficiency of carbon con version is relatively low, maintenance reaction temperature is difficult under conditions of no outer heat supply, and the technology is still in development.
The patent CN201010279560.7 of Xin Ao groups proposes a kind of multicompartment fluidized bed catalytic gasification high methane gas
The technique of body, gasification furnace is divided into synthesis gas and produces section, coal methanation section and synthesis gas methanation section.Make burning, gasification, methane
Change reaction and pyrolytic reaction segmentation is carried out, realize self-heat-supply reaction.But need to set multilayer air distribution plate in gasification furnace and overflow
Circulation road, structure in the stove is complicated, and gasification efficiency and methane production are relatively low, and the burning zone of fluidized-bed bottom easily makes ash melting
Reunite, form the slag of bulk, outlet and the gas distributor of gasification furnace are blocked, so as to influence the operation stability of device.
Because the gasification reaction of heat absorption and the methanation reaction of heat release are carried out in same reactor in above-mentioned technology, both
Ensure that kinetics considers the thermodynamical equilibrium of reaction again, which limits the operation temperature of reaction, cause as limit
It is relatively low to make the gasification reaction speed of reaction, and the methane equilibrium concentration of methanation balanced reaction is relatively low.Thus it can contemplate gas
Change and methanation reaction classification is carried out, quick catalytic gasification reaction generation synthesis gas is carried out in gasification reactor, and be pyrolyzed
Carry out being catalyzed pyrolysis and methanation reaction in methanator, generate the methane rich synthesis gas of low temperature.Therefore, it is possible to consider by
Gasifying and methanation reaction classification is carried out, study a kind of intensity of gasification height, gasification reaction speed is fast, methanation reaction degree height,
Technique is simple, the technology of stable and efficient catalytic coal gasifaction methane rich synthesis gas.
The content of the invention
Present invention mainly solves one of technical problem be efficiency of carbon con version and gasification low intensity, methane production in the prior art
Relatively low, the problem of energy consumption is higher and operation stability is poor, the present invention propose a kind of efficient catalytic coal gasifaction methane rich and closed
Into the device of gas, the device is made up of fluidized-bed gasification furnace and fluidized bed pyrolysis methanation furnace, and heat is passed through in fluidized-bed gasification furnace
Semicoke, circulation semicoke particle and gasifying agent are solved, carries out high-temp combustion and gasification reaction, generation high-temperature synthesis gas is entered by conduit
It is pyrolyzed in methanation furnace, contains CO in load2Under the catalyst action of trapping and mineral-bonded material, low temperature pyrogenation and methane are carried out
Change reaction, synthesis gas of the generation rich in methane.Material balance is realized, improves the intensity of gasification, efficiency of carbon con version and methane production,
And the device reduces system energy consumption.
The technical problems to be solved by the invention two are to provide a kind of with solving one of technical problem corresponding catalysis gas
Change reaction method.
To solve one of above-mentioned technical problem, the technical solution adopted by the present invention is as follows：A kind of efficient catalytic coal gasifaction
The device of methane rich synthesis gas processed, including material inlet 1, fluidized-bed gasification furnace 2, gasifying agent gas distributor 3, gasification outlet of still
4th, synthesis airway 5, fluidized bed pyrolysis methanation furnace 6, fluidized wind gas distributor 7, semicoke import 8, pyrolysis methanation furnace go out
Mouthfuls 9, cyclone separator 10, ash bucket 11, feed back straight tube 12, feeding back device 13, feed back import 14, separator 15, lower cinder notch 16,
Slag bucket 17 forms.It is characterized in that material inlet 1 is connected with fluidized bed pyrolysis methanation furnace 6, fluidized bed pyrolysis methanation furnace 6
Bottom is connected with the bottom of fluidized-bed gasification furnace 2, and fluidized gasification outlet of still 4 is by synthesizing airway 5 and fluidized bed pyrolysis
Methanation furnace 6 is connected, and fluidized gasification outlet of still 9 is connected with cyclone separator 10, the bottom of cyclone separator 10 connection ash
Bucket 11 and feed back straight tube 12, feeding back device 13 is connected by feed back import 14 with fluidized-bed gasification furnace 2, on cyclone separator 10
Side outlet is connected with separator 15, and the bottom of fluidized-bed gasification furnace 2 is connected by lower cinder notch 16 with slag bucket 17.
The position of described material inlet 1 is the 1/2~1/1 of the height of fluidized bed pyrolysis methanation furnace 6, material inlet 1
Angle and the angle that horizontal axis is in 0~75 °.
Described fluidized wind gas distributor 7 is located at the bottom of fluidized bed pyrolysis methanation furnace 6, in horizontally disposed, fluidized wind
Gas distributor 7 is provided with stomata, and stomata is circumferentially evenly arranged, provided with 10~30 circle stomatas, percent opening 0.1~5%.
The internal diameter of described fluidized bed pyrolysis methanation furnace 6 is more than fluidized-bed gasification furnace 2, is the internal diameter of fluidized-bed gasification furnace 2
1.1~3.0 times.
The position of described semicoke import 8 be fluidized-bed gasification furnace 2 bottom, be the height of fluidized-bed gasification furnace 2 1/8~
1/3。
Described gasifying agent gas distributor 3 is located at the bottom of fluidized-bed gasification furnace 2, is in be less than or equal to horizontal axis
60 ° of angle, center are provided with lower cinder notch 16, and the conical surface of gasifying agent gas distributor 3 is provided with stomata, stomata circumferentially uniform cloth
Put, provided with 5~20 circle stomatas, percent opening 0.1~5%.
The height of described synthesis airway 5 is more than the 3/4 of the height of fluidized bed pyrolysis methanation furnace 6, stretches to fluidisation
The bottom of bed pyrolysis methanation furnace 6, the internal diameter of described synthesis airway 5 for the internal diameter of fluidized bed pyrolysis methanation furnace 6 1/8~
1/3。
The internal diameter of described cyclone separator 11 is 1.5~2 times of the internal diameter of ash bucket 12.
The described bottom of feeding back device 13 is connected with returning charge wind, flies for what loose and fluidisation cyclone separator 10 separated
Ash.
The position of described feed back import 14 is located at the bottom of fluidized-bed gasification furnace 2, is the 1/8 of the height of fluidized-bed gasification furnace 2
~1/3, angle and the horizontal axis of feed back import 14 are in 15~75 ° of angle.
For solve the above problems two, the technical solution adopted by the present invention is as follows：A kind of efficient catalytic coal gasifaction system is rich
The method of methane synthesis gas, it is characterised in that comprise the following steps：The coal sample A of supported catalyst enters to become a mandarin by material inlet 1
Change in bed pyrolysis methanation furnace 6, with the high-temperature synthesis gas from synthesis airway 5, the fluidized wind C of fluidized wind gas distributor 7
Mixing contact, is pyrolyzed and methanation reaction, the semicoke particle after pyrolysis enter fluidized-bed gasification furnace 2 by semicoke import 8
In, the methane rich synthesis gas and coal ash particle of top pyrolysis methanation furnace outlet 9 enter in cyclone separator 10, are filled by feed back
The bottom that the coal ash particle separated is sent back to in the presence of 13 and returning charge wind D fluidized-bed gasification furnace 2 is put, in fluid bed gas
To change and combustion gasification reaction is carried out in stove 2, caused high-temperature synthesis gas is entered in fluidized bed pyrolysis methanation furnace 6 by conduit 5,
Melt the thick solid impurity particle G to reunite to fall into by lower cinder notch 16 in the slag bucket 17 of lower section, after the purifying and dedusting of cyclone separator 10
Gas-phase product tar E is separated by separator 15, obtain the synthesis gas F rich in methane.
Coal sample in described material inlet 1：Lignite, bituminous coal, anthracite, petroleum coke, biomass or its mixture, grain
Footpath is less than or equal to 10mm.
Described catalyst is selected from alkali metal, alkaline-earth metal, transition metal or its mixture；Described catalyst is to soak
The mode of stain method, dry pigmentation or ion-exchange is supported on raw coal；The load capacity of described catalyst accounts for the 0.1 of raw coal quality
~50%.
CO is added in described catalyst2Trap material (such as CaO, Ca (OH)2Deng) and mineral-bonded material, Ke Yishi
CO is fixed in existing stove2, and suppress catalyst inactivation.
The fluidized wind being passed through in described fluidized wind gas distributor 7 is inert gas, selected from nitrogen, argon gas, helium etc..
The gasifying agent being passed through in described gasifying agent gas distributor 3 is air, oxygen or oxygen-enriched air and vapor
Mixture.
400~600 DEG C of operation temperature, 3~6.5MPa of operating pressure, linear speed in described fluidized bed pyrolysis methanation furnace 6
Spend 0.1~5m/s.
0.5~1.2mol/mol of carbon ratio in described fluidized-bed gasification furnace 2,0.7~1.5mol/mol of steam/hydrocarbons ratio, behaviour
Make 800~1200 DEG C, 3~6.5MPa of operating pressure, 0.1~10m/s of linear velocity of temperature.
Described synthesis airway 5 is used to guide high-temperature synthesis gas caused by gasification in fluidized-bed gasification furnace to enter fluidized bed
It is pyrolyzed the bottom of methanation furnace 6.
The returning charge selection by winnowing of the described bottom of feeding back device 10 is from nitrogen, argon gas, vapor or its mixture.
Technical process is sketched used by using equipment of the invention：
By the coal sample of supported catalyst through material inlet enter fluidized bed pyrolysis methanation furnace in, with from synthesis airway
High-temperature synthesis gas and fluidized wind gas distributor fluidized wind mixing, carry out being catalyzed pyrolysis and methanation reaction, operation temperature
400~600 DEG C, 3.0~6.5MPa of pressure, generate CH4、CO2With the gas based on vapor, wherein CO2Gas can be by catalyst
In CO2Trapping material is fixed in catalyst, so as to improve the content of methane in exit gas.Fluidized bed pyrolysis methanation
The semicoke that pyrolysis is completed in stove is entered in fluidized-bed gasification furnace by semicoke import, pyrolysis methanation furnace outlet methane rich synthesis gas
In coal ash particle be passed through by cyclone separator and feeding back device in fluidized-bed gasification furnace, and from gasifying agent gas distributor
Gasifying agent carry out combustion gasification reaction, 800~1200 DEG C, 3~6.5MPa of pressure of operation temperature, generate CO, H2、CO2Deng high temperature
Gas, entered by synthesizing airway in fluidized bed pyrolysis methanation furnace, it is anti-for the pyrolysis in pyrolysis methanation furnace and methanation
Heat and reactant should be provided.Caused thick solid impurity particle drops into slag bucket by the lower cinder notch of bottom in fluidized-bed gasification furnace
In.After the methane rich synthesis gas of Cyclone outlet isolates tar by separator, follow-up wash cooling is sent to
In room, the synthesis gas rich in methane after desulfurization removing nitric is purified processing.
Advantages of the present invention is sketched：
1) using the combined catalytic gasification device of fluidized-bed gasification furnace and fluidized bed pyrolysis methanation furnace, in fluid bed heat
Solve and low temperature pyrogenation and methanation reaction are carried out in methanation furnace, be pyrolyzed complete semicoke and coal ash particle and enter fluidized-bed gasification furnace
The middle catalytic gasification reaction for carrying out high temperature, improves gasification reaction speed and efficiency of carbon con version, and in fluidized bed pyrolysis methanation furnace
It can reach higher methane equilibrium concentration and methane caused by taking full advantage of pyrolysis, realize the production of high gasification efficiency and methane
The target of rate.
2) high-temperature synthesis gas of fluidized gasification outlet of still is passed through fluidized bed pyrolysis methanation furnace by synthesizing airway
Bottom, flowed up again in stove after flowing out conduit, carry out catalytic production of methane reaction, extend high-temperature gas in methanation furnace
Residence time, the transmission of heat can be effectively facilitated and methanation reaction is reached low-temperature balance.
3) CO is added in the catalyst loaded2Trap material, such as CaO and Ca (OH)2Deng, or with the addition of mineral
Bonding material, CO can be realized in stove2Fixation, may advantageously facilitate transformationreation (CO+H2O=CO2+H2) balance move right
It is dynamic, so as to the H in effective regulating stove2/ CO ratios, are controlled in the range of suitable methanation reaction, and can improve outlet
The concentration of methane in gas, reduce the load of subsequent gases isolation of purified.
Combination using technical scheme by fluidized bed pyrolysis methanation furnace and gasification furnace, in fluidized bed pyrolysis
Catalysis pyrolysis and catalytic production of methane reaction are carried out in methanation furnace, complete semicoke and coal ash particle is pyrolyzed and is passed through fluidized gasification
Carry out being catalyzed combustion gasification reaction in stove, caused high-temperature synthesis gas is passed through the bottom of fluidized bed pyrolysis methanation furnace by conduit
Portion, realize the circulation of hot-fluid and logistics and reach the purpose made full use of.Gasification installation outlet efficiency of carbon con version can be made to reach 95%,
Methane content 75% in exiting syngas, while there is the characteristics of intensity of gasification is big, capacity usage ratio is high, simple and compact for structure,
Equipment investment and production cost are largely reduced, is had a good application prospect.
Brief description of the drawings
Fig. 1 is a kind of device schematic flow sheet of efficient catalytic coal gasifaction methane rich synthesis gas：
In Fig. 1,1 be material inlet, 2 be fluidized-bed gasification furnace, 3 be gasifying agent gas distributor, 4 be gasification outlet of still, 5
For synthesis airway, 6 be fluidized bed pyrolysis methanation furnace, 7 be fluidized wind gas distributor, 8 be semicoke import, 9 be pyrolysis first
Alkanisation outlet of still, 10 be cyclone separator, 11 be ash bucket, 12 be feed back straight tube, 13 be feeding back device, 14 be feed back import, 15
It is lower cinder notch for separator, 16,17 is slag bucket.A is the coal sample of supported catalyst；B is gasifying agent；C is fluidized wind；D is to return
Expect wind；E is tar；F is methane rich synthesis gas；G is thick slag.
The coal sample A of supported catalyst is entered in fluidized bed pyrolysis methanation furnace 6 by material inlet 1, and from synthesis gas
The fluidized wind C mixing contacts of the high-temperature synthesis gas of conduit 5, fluidized wind gas distributor 7, are pyrolyzed and methanation reaction, heat
Semicoke particle after solution is entered in fluidized-bed gasification furnace 2 by semicoke import 8, and top is pyrolyzed being the richest in for methanation furnace outlet 9
Alkane synthesis gas and coal ash particle enter in cyclone separator 10, by dividing whirlwind in the presence of feeding back device 13 and returning charge wind D
From the bottom that the coal ash particle separated in device 10 sends back to fluidized-bed gasification furnace 2, burnt in fluidized-bed gasification furnace 2
Gasification reaction, caused high-temperature synthesis gas are entered by conduit 5 and methanation reaction are participated in fluidized bed pyrolysis methanation furnace 6,
Melt the thick solid impurity particle G to reunite to fall into by lower cinder notch 16 in the slag bucket 17 of lower section, after the purifying and dedusting of cyclone separator 10
Gas-phase product tar E is separated by separator 15, obtain the synthesis gas F rich in methane of preliminary purification.
Below by embodiment, the invention will be further elaborated, but is not limited only to the present embodiment.
Embodiment
【Embodiment 1】
A kind of device of efficient catalytic coal gasifaction methane rich synthesis gas, fluidized bed pyrolysis methanation furnace internal diameter 1.0m,
Height 12m, material inlet are highly located at 2/3, fluidized-bed gasification furnace internal diameter 0.8m of fluidized bed pyrolysis methanation furnace height, height
15m, semicoke import are located at the 1/8 of fluidized-bed gasification furnace height, and feed back import is located at the 1/4 of fluidized-bed gasification furnace height, synthesis
The length that airway is stretched into fluidized bed pyrolysis methanation furnace is 9m, accounts for the 3/4 of methanation furnace height.
Inner Mongol lignite and 10%K are selected in experiment2CO3+ 5%CaO catalyst mixing, fluid bed heat is added from material inlet
Solve in methanation furnace, nitrogen is passed through in fluidized wind gas distributor makes raw material turbulent fluidization in stove, with the high temperature from conduit
Synthesis gas mixing contact, is pyrolyzed and methanation reaction, 500 DEG C, operating pressure 3.5MPa of operation temperature, generation are rich in methane
Synthesis gas, CH in exiting syngas4Concentration 75%, methane production 0.82Nm3/kg.Coal ash particle in methane rich synthesis gas leads to
Cross cyclone separator and feeding back device is collected and circulated and is sent into fluidized-bed gasification furnace, caused by fluidized bed pyrolysis methanation furnace
Semicoke particle is entered in fluidized-bed gasification furnace by semicoke import, and coal ash particle and semicoke particle from gasifying agent gas with being distributed
The oxygen and vapor of device carry out combustion gasification reaction, and carbon ratio control exists in 1.0mol/mol, vapor coal than control
1.2mol/mol, fluidized-bed gasification furnace operation temperature are 1000 DEG C, and operating pressure 3.5MPa, caused high-temperature synthesis gas passes through conjunction
Enter into airway in fluidized bed pyrolysis methanation furnace, provide reactant for the methanation reaction in stove and pyrolytic reaction and show
Heat, the efficiency of carbon con version of gasification installation outlet reach 96%.
【Embodiment 2】
A kind of device of efficient catalytic coal gasifaction methane rich synthesis gas, fluidized bed pyrolysis methanation furnace internal diameter 1.0m,
Height 12m, material inlet are highly located at 2/3, fluidized-bed gasification furnace internal diameter 0.8m of fluidized bed pyrolysis methanation furnace height, height
15m, semicoke import are located at the 1/8 of fluidized-bed gasification furnace height, and feed back import is located at the 1/4 of fluidized-bed gasification furnace height, synthesis
The length that airway is stretched into fluidized bed pyrolysis methanation furnace is 10m, accounts for the 5/6 of methanation furnace height.
Inner Mongol lignite and 10%K are selected in experiment2CO3+ 5%CaO catalyst mixing, fluid bed heat is added from material inlet
Solve in methanation furnace, nitrogen is passed through in fluidized wind gas distributor makes raw material turbulent fluidization in stove, with the high temperature from conduit
Synthesis gas mixing contact, is pyrolyzed and methanation reaction, 500 DEG C, operating pressure 3.5MPa of operation temperature, generation are rich in methane
Synthesis gas, CH in exiting syngas4Concentration 80%, methane production 0.89Nm3/kg.Coal ash particle in methane rich synthesis gas leads to
Cross cyclone separator and feeding back device is collected and circulated and is sent into fluidized-bed gasification furnace, caused by fluidized bed pyrolysis methanation furnace
Semicoke particle is entered in fluidized-bed gasification furnace by semicoke import, and coal ash particle and semicoke particle from gasifying agent gas with being distributed
The oxygen and vapor of device carry out combustion gasification reaction, and carbon ratio control exists in 1.0mol/mol, vapor coal than control
1.2mol/mol, fluidized-bed gasification furnace operation temperature are 1000 DEG C, and operating pressure 3.5MPa, caused high-temperature synthesis gas passes through conjunction
Enter into airway in fluidized bed pyrolysis methanation furnace, provide reactant for the methanation reaction in stove and pyrolytic reaction and show
Heat, the efficiency of carbon con version of gasification installation outlet reach 96%.
【Embodiment 3】
A kind of device of efficient catalytic coal gasifaction methane rich synthesis gas, fluidized bed pyrolysis methanation furnace internal diameter 1.0m,
Height 12m, material inlet are highly located at 2/3, fluidized-bed gasification furnace internal diameter 0.8m of fluidized bed pyrolysis methanation furnace height, height
15m, semicoke import are located at the 1/8 of fluidized-bed gasification furnace height, and feed back import is located at the 1/4 of fluidized-bed gasification furnace height, synthesis
The length that airway is stretched into fluidized bed pyrolysis methanation furnace is 9m, accounts for the 3/4 of methanation furnace height.
Inner Mongol lignite and 10%K are selected in experiment2CO3+ 10%CaO catalyst mixing, fluid bed heat is added from material inlet
Solve in methanation furnace, nitrogen is passed through in fluidized wind gas distributor makes raw material turbulent fluidization in stove, with the high temperature from conduit
Synthesis gas mixing contact, is pyrolyzed and methanation reaction, 500 DEG C, operating pressure 3.5MPa of operation temperature, generation are rich in methane
Synthesis gas, CH in exiting syngas4Concentration 85%, methane production 0.93Nm3/kg.Coal ash particle in methane rich synthesis gas leads to
Cross cyclone separator and feeding back device is collected and circulated and is sent into fluidized-bed gasification furnace, caused by fluidized bed pyrolysis methanation furnace
Semicoke particle is entered in fluidized-bed gasification furnace by semicoke import, and coal ash particle and semicoke particle from gasifying agent gas with being distributed
The oxygen and vapor of device carry out combustion gasification reaction, and carbon ratio control exists in 1.0mol/mol, vapor coal than control
1.2mol/mol, fluidized-bed gasification furnace operation temperature are 1000 DEG C, and operating pressure 3.5MPa, caused high-temperature synthesis gas passes through conjunction
Enter into airway in fluidized bed pyrolysis methanation furnace, provide reactant for the methanation reaction in stove and pyrolytic reaction and show
Heat, the efficiency of carbon con version of gasification installation outlet reach 98%.
【Embodiment 4】
A kind of device of efficient catalytic coal gasifaction methane rich synthesis gas, fluidized bed pyrolysis methanation furnace internal diameter 1.0m,
Height 12m, material inlet are highly located at 2/3, fluidized-bed gasification furnace internal diameter 0.8m of fluidized bed pyrolysis methanation furnace height, height
15m, semicoke import are located at the 1/8 of fluidized-bed gasification furnace height, and feed back import is located at the 1/4 of fluidized-bed gasification furnace height, synthesis
The length that airway is stretched into fluidized bed pyrolysis methanation furnace is 9m, accounts for the 3/4 of methanation furnace height.
Inner Mongol lignite and 10%K are selected in experiment2CO3+ 5%CaO catalyst mixing, fluid bed heat is added from material inlet
Solve in methanation furnace, nitrogen is passed through in fluidized wind gas distributor makes raw material turbulent fluidization in stove, with the high temperature from conduit
Synthesis gas mixing contact, is pyrolyzed and methanation reaction, 500 DEG C, operating pressure 3.5MPa of operation temperature, generation are rich in methane
Synthesis gas, CH in exiting syngas4Concentration 76%, methane production 0.86Nm3/kg.Coal ash particle in methane rich synthesis gas leads to
Cross cyclone separator and feeding back device is collected and circulated and is sent into fluidized-bed gasification furnace, caused by fluidized bed pyrolysis methanation furnace
Semicoke particle is entered in fluidized-bed gasification furnace by semicoke import, and coal ash particle and semicoke particle from gasifying agent gas with being distributed
The oxygen and vapor of device carry out combustion gasification reaction, and carbon ratio control exists in 1.2mol/mol, vapor coal than control
1.2mol/mol, fluidized-bed gasification furnace operation temperature are 1100 DEG C, and operating pressure 3.5MPa, caused high-temperature synthesis gas passes through conjunction
Enter into airway in fluidized bed pyrolysis methanation furnace, provide reactant for the methanation reaction in stove and pyrolytic reaction and show
Heat, the efficiency of carbon con version of gasification installation outlet reach 99%.
【Comparative example 1】
Using coal gasification reaction device in traditional two-step method preparing methane from coal technique, by taking the strange fixed-bed gasification furnace in Shandong as an example,
Experiment is Inner Mongol lignite from coal, operating pressure 3.5MPa, 800 DEG C of average operating temperature.In obtained exit gas component
CO+H2Content 55.4%, methane content only 12%, methane production 0.2Nm3/ kg, efficiency of carbon con version 90%.
【Comparative example 2】
Catalytic gasification reaction unit in the one-step method preparing methane from coal technique proposed using Exxon companies, from 10% carbon
Sour potassium catalyst, operating pressure 3.5MPa, 850 DEG C of superheated steam, 700 DEG C of operation temperature.Experiment is obtained in exit gas component
Methane content 19%, methane production 0.39Nm3/ kg, efficiency of carbon con version 85%.
【Comparative example 3】
Gasification reaction in the technique of the multicompartment fluidized bed catalytic gasification methane-rich gas proposed using Xin Ao groups is filled
Put, experiment is raw material from Inner Mongol lignite, loads 10% potassium carbonate catalyst, operating pressure 3.5MPa, operation temperature 700
℃.Methane content 8.4% in obtained exit gas component, methane production 0.15Nm3/ kg, efficiency of carbon con version 50%.
Claims (10)
1. a kind of device of efficient catalytic coal gasifaction methane rich synthesis gas, including material inlet (1), fluidized-bed gasification furnace
(2), gasifying agent gas distributor (3), gasification outlet of still (4), synthesis airway (5), fluidized bed pyrolysis methanation furnace (6), stream
Wind transmission gas distributor (7), semicoke import (8), pyrolysis methanation furnace outlet (9), cyclone separator (10), ash bucket (11), return
Expect straight tube (12), feeding back device (13), feed back import (14), separator (15), lower cinder notch (16), slag bucket (17) composition；Its
Be characterised by that material inlet (1) is connected with fluidized bed pyrolysis methanation furnace (6), fluidized bed pyrolysis methanation furnace (6) bottom with
Fluidized-bed gasification furnace (2) bottom is connected, and fluidized gasification outlet of still (4) is retired by synthesizing airway (5) and fluid bed heat
Alkanisation stove (6) is connected, and fluidized gasification outlet of still (9) is connected with cyclone separator (10), cyclone separator (10) bottom
Connection ash bucket (11) and feed back straight tube (12), feeding back device (13) are connected by feed back import (14) with fluidized-bed gasification furnace (2)
Connect, export above cyclone separator (10) and be connected with separator (15), fluidized-bed gasification furnace (2) bottom passes through lower cinder notch
(16) it is connected with slag bucket (17).
2. the device of efficient catalytic coal gasifaction methane rich synthesis gas according to claim 1, it is characterised in that described
Material inlet (1) position be fluidized bed pyrolysis methanation furnace (6) height 1/2~1, the angle and water of material inlet (1)
Flat axis is in 0~75 ° of angle.
3. the device of efficient catalytic coal gasifaction methane rich synthesis gas according to claim 1, it is characterised in that described
Fluidized wind gas distributor (7) be located at fluidized bed pyrolysis methanation furnace (6) bottom, in horizontally disposed, fluidized wind gas distribution
Device (7) is provided with stomata, and stomata is circumferentially evenly arranged, provided with 10~30 circle stomatas, percent opening 0.1~5%.
4. the device of efficient catalytic coal gasifaction methane rich synthesis gas according to claim 1, it is characterised in that described
Gasifying agent gas distributor (3) be located at the bottom of fluidized-bed gasification furnace (2), be in the folder less than or equal to 60 ° with horizontal axis
Angle, center are provided with lower cinder notch (16), and the conical surface of gasifying agent gas distributor (3) is provided with stomata, and stomata is circumferentially evenly arranged,
Provided with 5~20 circle stomatas, percent opening 0.1~5%.
5. the device of efficient catalytic coal gasifaction methane rich synthesis gas according to claim 1, it is characterised in that described
Synthesis airway (5) height be fluidized bed pyrolysis methanation furnace (6) height more than 3/4, it is retired to stretch to fluid bed heat
The bottom of alkanisation stove (6), the internal diameter of described synthesis airway (5) are the 1/8~1/ of fluidized bed pyrolysis methanation furnace (6) internal diameter
3。
6. the device of efficient catalytic coal gasifaction methane rich synthesis gas according to claim 1, it is characterised in that described
The position of feed back import (14) be located at fluidized-bed gasification furnace (2) bottom, be the 1/8~1/3 of fluidized-bed gasification furnace (2) height,
The angle of feed back import (14) and the angle that horizontal axis is in 15~75 °.
A kind of 7. method of efficient catalytic coal gasifaction methane rich synthesis gas, using any one described in claim 1~6
The device of efficient catalytic coal gasifaction methane rich synthesis gas, it is characterised in that mainly comprise the following steps：The coal sample (A) of supported catalyst
Entered by material inlet (1) in fluidized bed pyrolysis methanation furnace (6), with the high-temperature synthesis gas from synthesis airway (5), stream
Fluidized wind (C) the mixing contact of wind transmission gas distributor (7), is pyrolyzed and methanation reaction, the semicoke particle after pyrolysis leads to
Cross semicoke import (8) to enter in fluidized-bed gasification furnace (2), the methane rich synthesis gas and coal of top pyrolysis methanation furnace outlet (9)
Ash particle enters in cyclone separator (10), passes through the coal that will be separated in the presence of feeding back device (13) and returning charge wind (D)
Ash particle sends back to the bottom of fluidized-bed gasification furnace (2), and combustion gasification reaction is carried out in fluidized-bed gasification furnace (2), caused
High-temperature synthesis gas is entered in fluidized bed pyrolysis methanation furnace (6) by conduit (5), and the thick solid impurity particle (G) for melting reunion passes through
Lower cinder notch (16) is fallen into the slag bucket (17) of lower section, passes through separator by the gas-phase product after cyclone separator (10) dedusting
(15) tar (E) is separated, obtains the synthesis gas (F) rich in methane.
A kind of 8. method of efficient catalytic coal gasifaction methane rich synthesis gas according to claim 7, it is characterised in that
Described catalyst is selected from alkali metal, alkaline-earth metal, transition metal or its mixture；Described catalyst is with infusion process, dry
The mode of mixed method or ion-exchange is supported on raw coal；The load capacity of described catalyst accounts for the 0.1~50% of raw coal quality；
Contain CO in described catalyst2Material and mineral-bonded material are trapped,.
A kind of 9. method of efficient catalytic coal gasifaction methane rich synthesis gas according to claim 7, it is characterised in that
400~600 DEG C, 3~6.5MPa of operating pressure described of the interior operation temperature of fluidized bed pyrolysis methanation furnace (6), linear velocity 0.1~
5m/s；0.5~1.2mol/mol of carbon ratio, 0.7~1.5mol/mol of steam/hydrocarbons ratio in described fluidized-bed gasification furnace (2), behaviour
Make 800~1200 DEG C, 3~6.5MPa of operating pressure, 0.1~10m/s of linear velocity of temperature.
A kind of 10. method of efficient catalytic coal gasifaction methane rich synthesis gas according to claim 7, it is characterised in that
Described synthesis airway (5) is used to guide high-temperature synthesis gas caused by gasification in fluidized-bed gasification furnace (2) to enter fluid bed heat
Solve the bottom of methanation furnace (6).
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108373934A (en) * | 2018-05-18 | 2018-08-07 | 华北电力大学（保定） | Multiple types Biomass Gasification in Circulating Fluidized Bed reactor and its gasification process |
| CN110437881A (en) * | 2018-05-02 | 2019-11-12 | 国家能源投资集团有限责任公司 | Discharging device and system for the granular material that gasifies |
| CN111054274A (en) * | 2018-10-17 | 2020-04-24 | 中国石油化工股份有限公司 | Pulverized coal fluidized gasification and separation device and method |
| CN111621335A (en) * | 2020-06-02 | 2020-09-04 | 新奥科技发展有限公司 | Coal catalytic gasification system |
| CN113462434A (en) * | 2021-07-06 | 2021-10-01 | 中国科学院工程热物理研究所 | Gasification method and system with fly ash regasification function |
| CN113845950A (en) * | 2020-06-28 | 2021-12-28 | 中国石油化工股份有限公司 | Device and method for preparing methane by catalytic gasification of oxygen carrier coal |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102021037A (en) * | 2009-09-14 | 2011-04-20 | 新奥科技发展有限公司 | Method and apparatus for preparing methane by catalytic gasification of coal |
| CN104031703A (en) * | 2013-03-06 | 2014-09-10 | 中国石油天然气股份有限公司 | Method and device for preparation of natural gas synthesis gas from coal |
-
2016
- 2016-08-23 CN CN201610707698.XA patent/CN107760384B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102021037A (en) * | 2009-09-14 | 2011-04-20 | 新奥科技发展有限公司 | Method and apparatus for preparing methane by catalytic gasification of coal |
| CN104031703A (en) * | 2013-03-06 | 2014-09-10 | 中国石油天然气股份有限公司 | Method and device for preparation of natural gas synthesis gas from coal |
Non-Patent Citations (1)
| Title |
|---|
| JAMES G.SPEIGHT: "《The Chemistry and Technology of Coal, Third Editon》", 31 December 2013 * |
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| CN110437881A (en) * | 2018-05-02 | 2019-11-12 | 国家能源投资集团有限责任公司 | Discharging device and system for the granular material that gasifies |
| CN108373934A (en) * | 2018-05-18 | 2018-08-07 | 华北电力大学（保定） | Multiple types Biomass Gasification in Circulating Fluidized Bed reactor and its gasification process |
| CN111054274A (en) * | 2018-10-17 | 2020-04-24 | 中国石油化工股份有限公司 | Pulverized coal fluidized gasification and separation device and method |
| CN111621335A (en) * | 2020-06-02 | 2020-09-04 | 新奥科技发展有限公司 | Coal catalytic gasification system |
| CN113845950A (en) * | 2020-06-28 | 2021-12-28 | 中国石油化工股份有限公司 | Device and method for preparing methane by catalytic gasification of oxygen carrier coal |
| CN113845950B (en) * | 2020-06-28 | 2024-03-26 | 中国石油化工股份有限公司 | Device and method for preparing methane by catalytic gasification of oxygen carrier coal |
| CN113462434A (en) * | 2021-07-06 | 2021-10-01 | 中国科学院工程热物理研究所 | Gasification method and system with fly ash regasification function |
| CN113462434B (en) * | 2021-07-06 | 2022-08-02 | 中国科学院工程热物理研究所 | Gasification method and system with fly ash regasification function |
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