CN102021038B - Multilayer fluidized bed gasification furnace for preparing methane-rich gas by coal gasification - Google Patents
Multilayer fluidized bed gasification furnace for preparing methane-rich gas by coal gasification Download PDFInfo
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Abstract
The invention discloses a multilayer fluidized bed gasification furnace for preparing a methane-rich gas by coal gasification. The multilayer fluidized bed gasification furnace comprises a gasification furnace shell, at least two layers of gas distributors, a raw material inlet, a clinker outlet, a gasification agent inlet, a coal gas outlet, a first overflow device and a second overflow device, wherein the gas distributors are perpendicular to a longitudinal axis and arranged at different heights along the longitudinal axis in a perforated plate form to partition the internal space into an upper space, a middle space and a lower space; the clinker outlet and the gasification agent inlet are positioned at the bottom of the shell; the coal gas outlet is positioned on the top of the shell; and the first overflow device and the second overflow device are penetrated into the first gas distributor and the second gas distributor respectively and each of the first overflow device and the second overflow device is tubular, and has two open ends, so that a raw material flows from the upper space to the middle space through the first overflow device along a curved line and then flows to the lower space from the middle layer through the second overflow device.
Description
Technical field
In general, the present invention relates to gasification furnace, specifically, the present invention relates to the multicompartment fluidized bed gasification furnace that methane-rich gas is produced in a kind of coal gasification.
Background technology
The present invention relates to a kind of fine coal multicompartment fluidized bed gasification preparation and be rich in the multicompartment fluidized bed gasifying furnace device of methane gas.
China is the country of the oil-poor weak breath of rich coal, and along with society, rapid economy development, the China's natural gas demand is sharply soaring, and the ratio in energy resource structure increases sharply.And that domestic natural gas still is in exploration and development is early stage, and import also is in the starting stage, and deliverability seriously lags behind, and causes the natural gas imbalance between supply and demand to become increasingly conspicuous.Utilize the relatively large coal of china natural resources advantage, it is gasified produces combustion gas, can not only promote efficient, the clean utilization of coal; And existing natural gas line capable of using, with lower economic cost, effectively alleviate the imbalance between supply and demand of natural gas, this is the effective measure that coal resources fully utilize.
Common coal vaporizing system methane process, promptly coal at high temperature with oxygen (or air) and/or water vapour (H
2O) gasifying agent of forming carries out gasification reaction in the gasification furnace of individual layer, generate to contain a small amount of methane (CH
4) synthesis gas (mainly being hydrogen, carbon monoxide and carbon dioxide), carry out hydrosphere transformation and methanation operation afterwards, adopt two-step method to prepare methane.It is big, high to equipment requirements that this coal process has the gasification reaction energy consumption, and need three reaction units, technology than shortcomings such as complicacies.
It is the clean efficient a kind of important way utilized of coal that catalytic coal gasifaction prepares the methane technology, adopts the catalytic coal gasifaction technology, and coal is water vapour (H with main component under relatively low temperature
2O), hydrogen (H
2), the admixture of gas of carbon monoxide (CO) carries out gasification reaction under the catalytic action of catalyst, generate the methane (CH of high concentration
4).
At present; The catalytic coal gasifaction of mentioning in the related patent U.S. Patent No. prepares the methane technology and adopts cryogenic separation that the methane in the aerogenesis is separated with carbon monoxide, hydrogen; Hydrogen in the reacting gas and carbon monoxide are recycled in the gasification furnace; Make it in gasification furnace, to carry out methanation reaction and be converted into methane, thus the output of raising system methane.This catalytic coal gasifaction process can be accomplished in the gasification furnace of individual layer, but gasification reaction speed is low, the reaction time is long, and efficiency of carbon con version is lower, and gas separation system is invested high shortcoming; For satisfying the thermally equilibrated needs of reactor, need to advance the stove superheated steam and be heated to higher temperature, steam superheating system and heat-exchange system load are higher, less economical.
United States Patent (USP) 4,077,778 propose to adopt multistage fluidized bed to realize the catalytic gasification of coal, improve efficiency of carbon con version.The main fluidized-bed operating gas velocity is higher, and the part carbon granule is carried secretly to the secondary fluid bed, than carrying out gasification reaction under the low gas velocity, increases the solid phase time of staying, improves efficiency of carbon con version to greatest extent.Adopt multistage gasification can carbon utilisation rate be increased to more than 95% by 70～85% than the single-stage gasification.Multistage fluidized bed catalytic coal gasifaction process using multistage fluidized bed, equipment investment is high, and operation is complicated.
United States Patent (USP) 4,094,650 mention under catalytic alkali metal, can carbonaceous solids be gasified, preparation methane, catalyst need reclaim again and use.Reclaim water-soluble catalyst through multistage washing, lime slaking reclaims non-dissolubility catalyst.United States Patent (USP) 0277437 is at United States Patent (USP) 4; On 094,650 basis, adopt one-level to handle the alkali metal material is separated from the reactor solids residue; Simplified the base metal catalysts removal process; Improved the economy and the gross efficiency of catalysis gasification technique, but this recovery system is still complicated, recovery method is expensive.
U.S. Exxon company has carried out a large amount of experimental studies to coal one-step method system methane technology, and United States Patent (USP) 4318712 discloses the whole process flow of the direct methanation of a kind of coal, with coal in advance and after catalyst carries out premixed; Get into the coal gasification furnace reactor, the superheated steam of feeding is not only as gasifying agent, simultaneously as thermal source; Keep the reaction in furnace temperature; Control the interior temperature of stove about 700 ℃, 850 ℃ of superheat steam temperatures, gasification furnace reaction pressure 3.5MPa; Coal reacts with superheated steam under the effect of catalyst, directly obtains the product methane-rich gas.U.S. GPE company has carried out further research on the basis of EXXON technology; United States Patent (USP) 20070000177A1 also discloses the technology of the direct methanation of coal, and catalyst is alkali carbonate or alkali metal hydroxide, and gasifying agent is a steam; Its major technique characteristic is except adding efficiently methanation catalyst; Also added calcium oxide in the middle of the coal dust of reaction, the carbon dioxide that the absorption reaction process produces, thus further improve the content of methane.Owing to add the catalyst that promotes that methane generates; But high temperature is unfavorable for the generation of methane, and reaction temperature generally is controlled at about 700 ℃, and reaction speed is slow; The conversion ratio of carbon is low; Do not have outside heating system heat to be difficult to keep, and increased the catalyst recovery unit operations, the catalyst recovery effect directly influences production cost.
In addition, in order to make full use of heat, produce coal gas, United States Patent (USP) 5,064 is divided into pyrolysis section, gasification section, cooling section with fluidized-bed gasification furnace under the situation of 444 proposition pressurization steam gasifications, and each section separates with dividing plate.Pyrolysis section, gasification section are placed snake shape coil pipe (coil heat exchanger) in the gasification furnace, wherein feed 900 ℃～950 ℃ high-temperature gas such as the heating of the gas after fuel combustion coal dust, and gasification, pyrolysis institute calorific requirement are provided, and produce coal gas.This fluidized-bed gasification furnace can be for vertical, also can be horizontally, is gasifying agent with 700 ℃～800 ℃ superheated steams, and cooling section feeds saturated vapor, pneumatic charging.The time of staying of this device for prolonging coal dust, favourable solid phase processing, the heat energy utilization rate is high, but the reaction volume utilization rate in the gasification furnace is low, influences solid phase processing; Phosphorus content is higher in vertical heater when operation residue, is difficult to effective utilization; Compare with the gas-solid transmission of heat by contact, heat transfer rate is slow, the solid phase inequality of being heated in the bed; Equipment is numerous and diverse simultaneously, particularly horizontal chamber furnace (oven).
Therefore, the efficient gasification technology that utilizes of research ature of coal, the gasification installation that methane gas is rich in the corresponding low investment of exploitation, the simple coal gasification of technology preparation has far reaching significance.
Summary of the invention
Because above-mentioned situation, the present invention is devoted to provide a kind of low investment, technology simply to adopt the coal gasifying process to prepare the gasification installation that is rich in methane gas.
For realizing above-mentioned purpose, the present invention provides a kind of coal gasification to produce the multicompartment fluidized bed gasification furnace of methane-rich gas in first aspect, and this fluidized-bed gasification furnace comprises:
The gasification furnace housing, this housing has vertical longitudinal axis, and limits an inner space therein;
In the said inner space of said housing perpendicular to said longitudinal axis and at the two-layer at least gas distributor of arranging along the differing heights place of said longitudinal axis that is well plate format; Said two-layer at least gas distributor comprises first gas distributor and second gas distributor that is positioned at said first distributor below, and said first gas distributor and said second distributor are divided into upward sheaf space, space, intermediate layer and lower layer space with the said inner space of said housing;
Be arranged at the feed(raw material)inlet on the top, side of said housing, the said sheaf space of going up is led in this feed(raw material)inlet, is used for raw material is imported the said sheaf space of going up, and the general flow direction of said raw material is along said longitudinal axis from top to bottom;
Be positioned at the lime-ash outlet of the bottom of said housing;
Be positioned near the gasification agent inlet that gasifying agent gets into that is used for the side of said lime-ash outlet of bottom of said housing, the general flow direction of said gasifying agent is along said longitudinal axis from bottom to top;
Be positioned at the gas exit of said case top;
Connect first overflow mechanism that is provided with the tubular form that is both ends open on said first gas distributor; Connect second overflow mechanism that is provided with the tubular form that is both ends open on said second gas distributor; Said first overflow mechanism and second overflow mechanism are used to make said raw material along meander wire from top to bottom; Flow to space, said intermediate layer from the said sheaf space of going up through said first overflow mechanism, flow into said lower layer space by space, said intermediate layer through said second overflow mechanism again.
In a kind of preferred implementation of the present invention, on horizontal direction, be spaced from each other between the upper end of the lower end of said first overflow mechanism and said second overflow mechanism perpendicular to said longitudinal axis, descend to avoid material to lead directly to.
In a kind of preferred implementation of the present invention, the longitudinal middle part of said housing also is provided with the middle part charging aperture.
In a kind of preferred implementation of the present invention, vertical bottom of said housing also is provided with the underfeed mouth.
In a kind of preferred implementation of the present invention, also be provided with in said any space of going up in sheaf space, space, intermediate layer and the lower layer space and be used for the gas distributor of one deck at least that this space is further separated and connect this one deck gas distributor and overflow mechanism of arranging at least.
In a kind of preferred implementation of the present invention, in said housing, the below of said second gas distributor also is provided with the 3rd gas distributor.
In a kind of preferred implementation of the present invention, said the 3rd gas distributor is infundibulate.
In a kind of preferred implementation of the present invention, the angle of said overflow mechanism and horizontal direction is more than or equal to 30 °.
In a kind of preferred implementation of the present invention, the part that said overflow mechanism upper end exceeds gas distributor is a downflow weir, and the height of this downflow weir is held the decision of material amount by solid phase process time and bed, uses computes:
h＝4wt/[πD
2ρ(1-ε)]
The height of weir plate of h---certain layer, unit is m
This layer of w---solid particle inlet amount, unit is kg/h
This layer of t----solid phase process time, unit is h
The internal diameter of this layer of D----body of heater, unit are m
The density of ρ----this layer bed under operating condition, unit is kg/m
3
ε-----porosity of this layer bed under operating condition.
In a kind of preferred implementation of the present invention,
Distance between two adjacent gas distributors is held the height decision of material amount by height that is in the overflow pipe between them and bed, uses computes:
H＝H
1+h
1-h
2
Wherein
Distance between two adjacent gas distributors of H----, unit is m;
H
1The height of the overflow pipe between---be in two gas distributors, unit are m;
h
1The bed of material that----is between two gas distributors is held the height of material amount, and unit is m;
h
2----is in the bed depth of imbedding of overflow pipe between two gas distributors, and unit is m.
In second aspect of the present invention, provide a kind of coal gasification to produce the multicompartment fluidized bed gasification furnace of methane-rich gas, this fluidized-bed gasification furnace comprises:
The gasification furnace housing, this housing has vertical longitudinal axis, and limits an inner space therein;
One deck of in the said inner space of said housing, arranging perpendicular to said longitudinal axis is the gas distributor of well plate format, and said gas distributor is divided into upward sheaf space and lower layer space with the said inner space of said housing;
Be arranged at the feed(raw material)inlet on the top, side of said housing, the said sheaf space of going up is led in this feed(raw material)inlet, is used for raw material is imported the said sheaf space of going up, and the general flow direction of said raw material is along said longitudinal axis from top to bottom;
Be positioned at the lime-ash outlet of the bottom of said housing;
Be positioned near the gasification agent inlet that gasifying agent gets into that is used for the side of said lime-ash outlet of bottom of said housing, the general flow direction of said gasifying agent is along said longitudinal axis from bottom to top;
Be positioned at the gas exit of said case top;
Connect the overflow mechanism that is provided with the tubular form that is both ends open on the said gas distributor, said overflow mechanism is used to make said raw material from top to bottom, flows to said lower layer space from the said sheaf space of going up through said overflow mechanism.
Compare with the fluidized-bed gasification furnace (needing to be provided with two-layer at least gas distributor) that first aspect of the present invention provides; The fluidized-bed gasification furnace that second aspect of the present invention provides is minimum only need to be provided with one deck gas distributor, is divided into sheaf space and lower layer space with the inner space with gasification furnace.
The fluidized-bed gasification furnace that provides according to a second aspect of the invention can have the one or more characteristics in the preferred feature of the fluidized-bed gasification furnace that provides according to a first aspect of the invention.
Use the technical process summary that equipment of the present invention adopts (withThe fluidized-bed gasification furnace that first aspect of the present invention provides is an example
)
Under the effect of rotary feeder, the impregnated catalyst coal dust is added three-layer type fluidized-bed gasification furnace intermediate layer space B (catalytic gasification district); Pyrolysis section adds raw coal from reactor top, passes through sheaf space A on the multicompartment fluidized bed gasification furnace (partial thermal decomposition district) successively, intermediate layer space B (catalytic gasification district) and orlop C (residue gasification zone).The partial thermal decomposition district, the cold coal dust of elevated temperature heat gas heating charging that reaction produces makes it to take place partial thermal decomposition, generates products such as the pyrolysis gas that is rich in methane and tar.Afterwards, the coal dust through partial thermal decomposition gets into the catalytic gasification district, reactions such as generation catalytic gasification, methanation under the effect of catalyst, generation methane, carbon monoxide, available gas composition and carbon dioxide, a spot of hydrogen sulfide and ammonia etc. such as hydrogen.Fully the coal residue of reaction does not get into the residue gasification zone; Effect gasified at oxygen and water vapour generates gases such as carbon monoxide, hydrogen, carbon dioxide; And carbon monoxide, hydrogen get into epimere catalytic gasification district; Methanation reaction takes place under the effect of catalyst, increase system's methane production, the high-temperature vapor of generation provides the part heat for the catalytic gasification district.Control residue gasification zone process conditions; Realize the separation of ash, Jiao, catalyst, the high-temperature lower part divided catalyst is gaseous form and gets into epimere catalytic gasification district participation gasification reaction, gaseous catalyst entering part pyrolysis zone; The reduction of temperature makes it to exist form to change; Separate with gaseous product, stay and continue to participate in gasification reaction in the stove, realize the recycle of stove inner catalyst.The gasification furnace exit gas is through isothermal dust-filtering unit, and dust returns gasification furnace and carries out gasification reaction, and gas carries out gas-liquid separation through the gas-liquid cold separation unit, obtains low temperature tar and raw gas.Get into gas cleaning plant afterwards, remove sour gas such as carbon dioxide and hydrogen sulfide, obtain being rich in the coal gas of methane.
Advantage brief introduction of the present invention
(1) keep catalytic gasification characteristic and advantage, obtained the methane of high level, overcome the difficult point of independent catalytic gasification, more high like reaction time lime-ash carbon content long, that discharge;
(2) multilayer coupled gasification; Sheaf space A on the multicompartment fluidized bed gasification furnace (partial thermal decomposition district) utilizes the surplus temperature of catalytic gasification aerogenesis to heat the fine coal that has just got into, and carries out partial thermal decomposition; Produce products such as methane gas, under the condition that does not increase energy consumption, increased methane and tar; The catalytic gasification main reaction takes place in the intermediate layer space B; Orlop C when feeding gasifying agent, feeds the small amount of oxygen residual residue that gasifies, and through the heat that burning, gasification to residue provide catalytic gasification to need, provides hydrogen and CO to help catalytic gasification simultaneously and reacts;
(3) prepare methane with two-step method and compare, this device integrates three reactors, realizes logistics coupling, heat coupling, and confession reaction heat reduces the energy consumption of superheated steam, has solved the problem of residue carbon containing; Prolong mean residence time, increased the gas production capacity, improved efficiency of carbon con version.
See from whole process that (4) utilize this multicompartment fluidized bed gasification furnace gasification preparation to be rich in methane gas, the thermal efficiency is higher, the solid phase working depth is higher, and methane content is higher in the gaseous product, and equipment is simplified, and is easy to operate.
(5) these multi-compartment bed the superiors generate restrain tar to change into and promote tar to generate, and reduce catalyst amount, reduce the catalyst cost; Simultaneously can utilize the part trade waste, improve methane content as the catalyst raw material.
Description of drawings
Fig. 1 is the structure chart of one embodiment of the present of invention;
Fig. 2, Fig. 3, Fig. 4 are respectively the structure chart of other each embodiment of the present invention.
The specific embodiment
Shown in each accompanying drawing, first aspect of the present invention provides a kind of coal gasification to produce the multicompartment fluidized bed gasification furnace of methane-rich gas, and this fluidized-bed gasification furnace comprises:
In the said inner space of said housing 3 perpendicular to said longitudinal axis and at the two-layer at least gas distributor of arranging along the differing heights place of said longitudinal axis 2 that is well plate format; Said two-layer at least gas distributor 2 comprises first gas distributor and second gas distributor that is positioned at said first distributor below, and said first gas distributor and said second distributor are divided into upward sheaf space A, intermediate layer space B and lower layer space C with the said inner space of said housing;
Be arranged at the feed(raw material)inlet 4 on the top, side of said housing, the said sheaf space A of going up is led in this feed(raw material)inlet, is used for raw material is imported the said sheaf space A of going up, and the general flow direction of said raw material is along said longitudinal axis from top to bottom;
Be positioned at the lime-ash outlet 7 of the bottom of said housing 3;
The said lime-ash that is positioned at the bottom of said housing exports near 7 the gasification agent inlet that is used for the gasifying agent entering in side, and the general flow direction of said gasifying agent is along said longitudinal axis from bottom to top;
Be positioned at the gas exit at said housing 3 tops;
Connect first overflow mechanism 1 that is provided with the tubular form that is both ends open on said first gas distributor; Connect second overflow mechanism 1 that is provided with the tubular form that is both ends open on said second gas distributor; Said first overflow mechanism and second overflow mechanism are used to make said raw material along meander wire from top to bottom; Flow to said intermediate layer space B from the said sheaf space A that goes up through said first overflow mechanism, flow into said lower layer space C by said intermediate layer space B through said second overflow mechanism again.
In a kind of preferred implementation of the present invention, on horizontal direction, be spaced from each other between the upper end of the lower end of said first overflow mechanism and said second overflow mechanism perpendicular to said longitudinal axis, descend to avoid material to lead directly to.
In a kind of preferred implementation of the present invention, the longitudinal middle part of said housing also is provided with middle part charging aperture 4.
In a kind of preferred implementation of the present invention, vertical bottom of said housing also is provided with underfeed mouth 5 (see figure 2)s.
In a kind of preferred implementation of the present invention, also be provided with in said any space of going up among sheaf space A, intermediate layer space B and the lower layer space C and be used for the gas distributor of one deck at least that this space is further separated and connect this one deck gas distributor and overflow mechanism of arranging at least.
In a kind of preferred implementation of the present invention, in said housing, the below of said second gas distributor also is provided with the 3rd gas distributor.
In a kind of preferred implementation of the present invention, said the 3rd gas distributor is the infundibulate (see figure 3).
In a kind of preferred implementation of the present invention, the angle of said overflow mechanism and horizontal direction is more than or equal to 30 °.
Second aspect of the present invention provides a kind of coal gasification to produce the multicompartment fluidized bed gasification furnace (not shown) of methane-rich gas, and this fluidized-bed gasification furnace comprises:
The gasification furnace housing, this housing has vertical longitudinal axis, and limits an inner space therein;
One deck of in the said inner space of said housing, arranging perpendicular to said longitudinal axis is the gas distributor of well plate format, and said gas distributor is divided into upward sheaf space and lower layer space with the said inner space of said housing;
Be arranged at the feed(raw material)inlet on the top, side of said housing, the said sheaf space of going up is led in this feed(raw material)inlet, is used for raw material is imported the said sheaf space of going up, and the general flow direction of said raw material is along said longitudinal axis from top to bottom;
Be positioned at the lime-ash outlet of the bottom of said housing;
Be positioned near the gasification agent inlet that gasifying agent gets into that is used for the side of said lime-ash outlet of bottom of said housing, the general flow direction of said gasifying agent is along said longitudinal axis from bottom to top;
Be positioned at the gas exit of said case top;
Connect the overflow mechanism that is provided with the tubular form that is both ends open on the said gas distributor, said overflow mechanism is used to make said raw material from top to bottom, flows to said lower layer space from the said sheaf space of going up through said overflow mechanism.
Compare with the fluidized-bed gasification furnace (needing to be provided with two-layer at least gas distributor) that first aspect of the present invention provides; The fluidized-bed gasification furnace that second aspect of the present invention provides is minimum only need to be provided with one deck gas distributor, so that the gasification furnace inner space is divided into sheaf space and lower layer space.
The fluidized-bed gasification furnace that provides according to a second aspect of the invention can have the one or more characteristics in the preferred feature of the fluidized-bed gasification furnace that provides according to a first aspect of the invention.
Referring to Fig. 1; First aspect of the present invention provides a kind of equipment for gasification; Can be applied to the gasification of multicompartment fluidized bed coal produces in the methane-rich gas system; This equipment is the multicompartment fluidized bed gasification furnace, comprising: go up sheaf space A (partial thermal decomposition district), intermediate layer space B (catalytic gasification district), orlop C (residue gasification zone).
Raw coal is through the charging aperture 4 entering part pyrolysis zone of sheaf space A on the multicompartment fluidized bed, and the cold coal dust of elevated temperature heat gas heating charging through the lower end reaction produces makes it to take place partial thermal decomposition.Former pyrolysis of coal obtains being rich in pyrolysis gas, tar and the semicoke of methane.Gaseous catalyst gets into goes up sheaf space A (partial thermal decomposition district), and the reduction of temperature makes it to exist form to change, and separates with gaseous product, stays and continues to participate in gasification reaction in the stove, realizes the recycle of stove inner catalyst.
Coal and the mixture of catalysts charging aperture 4 through the intermediate layer space B gets into gasification furnace catalytic gasification districts, and mixes through the coal dust of overflow pipe 1 from the partial thermal decomposition of last sheaf space A, under the effect of catalyst and the gasifying agent generating gasification react generation CH
4, CO, H
2Deng available gas composition and CO
2, a spot of H
2S and NH
3Deng.Key reaction is following:
2C+2H
2O→2H
2+2CO (1)
CO+H
2O→CO
2+H
2 (2)
3H
2+CO→CH
4+H
2O (3)
C+2H
2→CH
4 (4)
Orlop C (residue gasification zone), the CO of generation, H
2, can get into epimere intermediate layer space B (catalytic gasification district), methanation reaction takes place under the effect of catalyst, increase system's methane production, the high-temperature vapor that produces in addition is intermediate layer space B (catalytic gasification district), and partial reaction institute calorific requirement is provided.
Fully the coal residue of reaction does not get into the residue gasification zone, at O
2Generate CO, H with the effect gasified of water vapour
2, CO
2Deng gas.Key reaction is as follows:
C+O
2→CO
2 (5)
C+CO
2→2CO (6)
C+H
2O→CO+H
2 (7)
CO+H
2O→CO
2+H
2?(8)
CO, H that gasification furnace residue gasification zone C produces
2, can get into epimere intermediate layer space B (catalytic gasification district), methanation reaction takes place under the effect of catalyst; Increase system methane production; High-temperature gas that produces in addition and steam have reduced the lime-ash carbon content for the catalytic gasification district provides the part heat, improve charging coal dust comprehensive utilization ratio.
Orlop C (residue gasification zone); Temperature is higher; The part catalyst evaporates into intermediate layer space B (catalytic gasification district) with gaseous form; Recycling of fluid bed inner catalyst can reduce catalyst addition in the initial coal dust, reduces the burden of catalyst recovery system, or need not to dispose in addition catalyst recovery system.
Gasifying agent superheated steam and minor amounts of oxygen get into the residue gasification zone from gasification furnace bottom, burn with residue, gasification reaction, and (catalytic gasification district) provides required heat for the intermediate layer space B.
Platoon slag equipment under the multicompartment fluidized bed gasification furnace is used to discharge the lime-ash after gasifying in the residue gasification zone.
The high-temperature furnace gas that the multicompartment fluidized bed gasification furnace produces is discharged by furnace roof, gets into the later separation cleaning procedure.
Embodiment 1:
Referring to Fig. 2, on the basis of structure chart 1, as the heat that only depends on residue gasification to produce is difficult to satisfy the temperature required requirement of catalytic gasification, can on the body of heater 3 of the orlop C of multicompartment fluidized bed, establish a charging aperture 5, adds a small amount of raw coal to the residue gasification zone through this charging aperture.
Embodiment 2:
Referring to Fig. 3, on the basis of structure chart 1,, can change the distribution grid of multicompartment fluidized bed orlop C for satisfying the needs of ash discharge or process condition, use the infundibulate distribution grid, regulate and control ash discharge gas speed and fluidizing gas velocity respectively through air inlet 6,7.
Embodiment 3:
Referring to Fig. 4, on the basis of structure chart 1,, realize the continous-stable overflow between bed for fear of playing a reversed role of gas, be convenient to control the excess flow of material simultaneously, can use other forms of overflow pipe, like the plug formula overflow pipe of band mechanical driving device.Position through mechanical driving device adjusting plug 8 changes gas direction and feed opening cross-sectional sizes, realizes smooth overflow.
Relative position about overflow mechanism and gas distributor:
1. overflow pipe can be installed in place, any horizontal cross-sections of gas distributor 2, can vertically install, and also tiltable is installed, with the angle of horizontal plane more than or equal to 30 °; Be short-circuited when avoiding solid particle between two overflow pipes, to flow, the outlet of upper end overflow pipe should keep certain distance in the horizontal direction with the import of lower end overflow pipe, avoids distance too little (all being placed in the gas distributor center like two overflow pipes) as far as possible.
2. the height of downflow weir (the overflow pipe upper end exceeds the part of gas distributor) is held the decision of material amount by solid phase process time and bed, uses computes:
h＝4wt/[πD
2ρ(1-ε)]
H---layer of height of weir plate, unit is m
This layer of w---solid particle inlet amount, unit is kg/h
This layer of t----solid phase process time, unit is h
The internal diameter of this layer of D----body of heater, unit are m
The density of ρ----this layer bed under operating condition, unit is kg/m
3
ε-----porosity of this layer bed under operating condition
3. the distance between two adjacent gas distributors is held the height decision of material amount by height that is in the overflow pipe between them and bed, uses computes:
H＝H
1+h
1-h
2
Wherein
Distance between two adjacent gas distributors of H----, unit is m;
H
1The height of the overflow pipe between---be in two gas distributors, unit are m;
h
1The bed of material that----is between two gas distributors is held the height of material amount, and unit is m;
h
2----is in the bed depth of imbedding of overflow pipe between two gas distributors, and unit is m.
Core technology point of the present invention:
1, the integraty of multicompartment fluidized bed: gasifying agent feeds from the gasification furnace bottom, and pyrolysis section adds raw coal from reactor top, successively last sheaf space A, intermediate layer space B, the orlop C of process multicompartment fluidized bed.The last sheaf space A (partial thermal decomposition district) of multicompartment fluidized bed, the cold coal dust of elevated temperature heat gas heating charging that reaction produces makes it to take place partial thermal decomposition, generates and is rich in CH
4Product such as pyrolysis gas and tar.Afterwards, reactions such as catalytic gasification, methanation take place in the intermediate layer space B (catalytic gasification district) through the coal dust of partial thermal decomposition gets into multicompartment fluidized bed under the effect of catalyst, generate CH
4, CO, H
2Deng available gas composition and CO
2, a spot of H
2S and NH
3Deng.The coal residue that does not fully react gets into the orlop C (residue gasification zone) of multicompartment fluidized bed, at O
2Generate CO, H with the effect gasified of water vapour
2, CO
2Deng gas.
2, the tight association of multicompartment fluidized bed orlop C and intermediate layer space B: at the orlop C (residue gasification zone) of multicompartment fluidized bed; Residue and oxygen reaction send a large amount of heats; Be the intermediate layer space B, the catalytic gasification section provides required heat; Reduce the lime-ash carbon content, improve charging coal dust comprehensive utilization ratio; Simultaneously; At high temperature the part catalyst evaporates into the intermediate layer space B (catalytic gasification district) of multicompartment fluidized bed with gaseous form; Recycling of fluid bed inner catalyst can reduce catalyst addition in the initial coal dust; Reduce the burden of catalyst recovery system, or need not to dispose in addition catalyst recovery system; Gasification furnace residue gasification zone, multicompartment fluidized bed orlop C, the CO of generation, H
2, can get into multicompartment fluidized bed intermediate layer space B (catalytic gasification district), methanation reaction takes place under the effect of catalyst, increase system's methane production, the high-temperature vapor that produces in addition provides the part heat for the catalytic gasification district.
3, the selection of the charging aperture of multicompartment fluidized bed: according to the needs of system thermal balance and process condition, except that the superiors' charging aperture of multicompartment fluidized bed, can be in the intermediate layer, the diverse location place of orlop body of heater 3 sets up charging aperture.
4, the number of plies of multi-compartment bed: can be according to the needs of the time of staying and process condition; Partial thermal decomposition district, catalytic gasification district, residue gasification zone with the multicompartment fluidized bed gasification furnace; Be divided into single or multiple lift respectively, each interlayer separates with gas distributor 2, and overflow mechanism 1 is installed.
5, overflow mechanism 1: can be the mechanical type overflow mechanism, like the lower end at overflow pipe plug, valve are installed, can be the Pneumatic-control type overflow mechanism also, like straight tube, and conical pipe, L shaped valve.
6, gas distributor 2: the gas distributor 2 of multicompartment fluidized bed middle and upper part fixed weir pipe 1 can be dull and stereotyped distribution grid, tilt distribution plate or infundibulate distribution grid, or their combining form.The gas distributor 2 of multicompartment fluidized bed lower gas import department can be dull and stereotyped distribution grid, tilt distribution plate, infundibulate distribution grid, or the gas distribution grid of band jet.
7, this multicompartment fluidized bed gasification furnace can be in normal pressure, add and depress use.
Technical problem that the present invention solves and beneficial effect compared with prior art
The purpose of this invention is to provide a kind of coal gasification preparation and be rich in the multicompartment fluidized bed gasification furnace of methane gas; This gasification furnace is realized the continous-stable overflow of multicompartment fluidized bed interlayer through overflow mechanism 1; Pyrolysis, gasification, burning are coupled in the multicompartment fluidized bed; The realization classification transforms, and is that energy distribution is carried out at the center with catalytic gasification system methane, realizes the price of gold exploitation.
At first, with United States Patent (USP) 4,077,778 multistage fluidized bed is compared, and in (one-level) fluid bed, has prolonged the solid phase time of staying, improves efficiency of carbon con version to greatest extent, reduces equipment investment, simultaneously easy operating;
Secondly; Compare with the device in other patents; The gasification reaction of the residue gasification zone through multi-compartment bed orlop C provides hydrogen and carbon monoxide to the catalytic gasification district in intermediate layer, promotes the carrying out of methanation reaction, need not separating hydrogen gas and CO gas piece-rate system; Significantly reduce equipment investment, simplify the operation; Simultaneously at multi-compartment bed orlop C; Feed gasifying agent and minor amounts of oxygen; Part residue burning provides reaction required part heat to the catalytic gasification reaction of intermediate layer space B, both can reduce the import steam temperature; Reduce steam superheating system and heat-exchange system load, also solved the problem of residue carbon containing.
In addition, the methane that sheaf space A pyrolysis section generates on the multi-compartment bed, the gasification furnace of directly overflowing is avoided oxidation, increases methane content in the gas-phase product, can obtain through pyrogenous origin multiple other products simultaneously.From the angle of heat, made full use of heat energy from the gas of intermediate layer space B, have the higher thermal efficiency, also bring convenience for the postorder treatment system.
At last, with regard to the utilization of catalyst, these multi-compartment bed the superiors generate restrain tar to change into and promote tar to generate, and reduce catalyst amount, reduce the catalyst cost; Simultaneously can utilize the part trade waste, improve methane content as the catalyst raw material.
Claims (15)
1. the multicompartment fluidized bed gasification furnace of methane-rich gas is produced in coal gasification, and this fluidized-bed gasification furnace comprises:
The gasification furnace housing, this housing has vertical longitudinal axis, and limits an inner space therein;
In the said inner space of said housing perpendicular to said longitudinal axis and at the two-layer at least gas distributor of arranging along the differing heights place of said longitudinal axis that is well plate format; Said two-layer at least gas distributor comprises first gas distributor and second gas distributor that is positioned at said first distributor below, and said first gas distributor and said second distributor are divided into upward sheaf space, space, intermediate layer and lower layer space with the said inner space of said housing;
Be arranged at the feed(raw material)inlet on the top, side of said housing, the said sheaf space of going up is led in this feed(raw material)inlet, is used for raw material is imported the said sheaf space of going up, and the general flow direction of said raw material is along said longitudinal axis from top to bottom;
Be positioned at the lime-ash outlet of the bottom of said housing;
Be positioned near the gasification agent inlet that gasifying agent gets into that is used for the side of said lime-ash outlet of bottom of said housing, the general flow direction of said gasifying agent is along said longitudinal axis from bottom to top;
Be positioned at the gas exit of said case top;
Connect first overflow mechanism that is provided with the tubular form that is both ends open on said first gas distributor; Connect second overflow mechanism that is provided with the tubular form that is both ends open on said second gas distributor; Said first overflow mechanism and second overflow mechanism are used to make said raw material along meander wire from top to bottom; Flow to space, said intermediate layer from the said sheaf space of going up through said first overflow mechanism, flow into said lower layer space by space, said intermediate layer through said second overflow mechanism again.
2. fluidized-bed gasification furnace as claimed in claim 1 is characterized in that, on the horizontal direction perpendicular to said longitudinal axis, is spaced from each other between the upper end of the lower end of said first overflow mechanism and said second overflow mechanism, descends to avoid material to lead directly to.
3. fluidized-bed gasification furnace as claimed in claim 1 is characterized in that, the longitudinal middle part of said housing also is provided with the middle part charging aperture.
4. fluidized-bed gasification furnace as claimed in claim 1 is characterized in that, vertical bottom of said housing also is provided with the underfeed mouth.
5. fluidized-bed gasification furnace as claimed in claim 1; It is characterized in that, also be provided with in said any space of going up in sheaf space, space, intermediate layer and the lower layer space and be used for the gas distributor of one deck at least that this space is further separated and connect this one deck gas distributor and overflow mechanism of arranging at least.
6. fluidized-bed gasification furnace as claimed in claim 1 is characterized in that, in said housing, the below of said second gas distributor also is provided with the 3rd gas distributor.
7. fluidized-bed gasification furnace as claimed in claim 6 is characterized in that, said the 3rd gas distributor is infundibulate.
8. like each described fluidized-bed gasification furnace of claim 1 to 7, it is characterized in that the angle of said overflow mechanism and horizontal direction is more than or equal to 30 °.
9. like each described fluidized-bed gasification furnace of claim 1 to 7, it is characterized in that,
The part that said overflow mechanism upper end exceeds gas distributor is a downflow weir, and the height of this downflow weir is held the decision of material amount by solid phase process time and bed, uses computes:
h＝4wt/[πD
2ρ(1-ε)]
The height of weir plate of h---certain layer, unit is m;
This layer of w---solid particle inlet amount, unit is kg/h;
This layer of t----solid phase process time, unit is h;
The internal diameter of this layer of D----body of heater, unit are m;
The density of ρ----this layer bed under operating condition, unit is kg/m
3
ε-----porosity of this layer bed under operating condition.
10. like each described fluidized-bed gasification furnace of claim 1 to 7, it is characterized in that,
Distance between two adjacent gas distributors is held the height decision of material amount by height that is in the overflow pipe between them and bed, uses computes:
H＝H
1+h
1-h
2
Wherein
Distance between two adjacent gas distributors of H----, unit is m;
H
1The height of the overflow pipe between---be in two gas distributors, unit are m;
h
1The bed of material that----is between two gas distributors is held the height of material amount, and unit is m;
h
2----is in the bed depth of imbedding of overflow pipe between two gas distributors, and unit is m.
11. the multicompartment fluidized bed gasification furnace of methane-rich gas is produced in a coal gasification, this fluidized-bed gasification furnace comprises:
The gasification furnace housing, this housing has vertical longitudinal axis, and limits an inner space therein;
One deck of in the said inner space of said housing, arranging perpendicular to said longitudinal axis is the gas distributor of well plate format, and said gas distributor is divided into upward sheaf space and lower layer space with the said inner space of said housing;
Be arranged at the feed(raw material)inlet on the top, side of said housing, the said sheaf space of going up is led in this feed(raw material)inlet, is used for raw material is imported the said sheaf space of going up, and the general flow direction of said raw material is along said longitudinal axis from top to bottom;
Be positioned at the lime-ash outlet of the bottom of said housing;
Be positioned near the gasification agent inlet that gasifying agent gets into that is used for the side of said lime-ash outlet of bottom of said housing, the general flow direction of said gasifying agent is along said longitudinal axis from bottom to top;
Be positioned at the gas exit of said case top;
Connect the overflow mechanism that is provided with the tubular form that is both ends open on the said gas distributor, said overflow mechanism is used to make said raw material from top to bottom, flows into said lower layer space from the said sheaf space of going up through said overflow mechanism.
12. fluidized-bed gasification furnace as claimed in claim 11 is characterized in that, the longitudinal middle part of said housing also is provided with the middle part charging aperture.
13. fluidized-bed gasification furnace as claimed in claim 11 is characterized in that, vertical bottom of said housing also is provided with the underfeed mouth.
14. fluidized-bed gasification furnace as claimed in claim 11; It is characterized in that, also be provided with in said any space of going up in sheaf space and the lower layer space and be used for the gas distributor of one deck at least that this space is further separated and connect this one deck gas distributor and overflow mechanism of arranging at least.
15., it is characterized in that the angle of said overflow mechanism and horizontal direction is more than or equal to 30 ° like each described fluidized-bed gasification furnace of claim 11 to 14.
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| CN 200910170387 CN102021038B (en) | 2009-09-14 | 2009-09-14 | Multilayer fluidized bed gasification furnace for preparing methane-rich gas by coal gasification |
| PCT/CN2010/001410 WO2011029285A1 (en) | 2009-09-14 | 2010-09-14 | Multi-layer fluidized bed gasifier |
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| CN102329651B (en) * | 2011-08-26 | 2014-03-26 | 北京大学深圳研究生院 | Three-stage gasification device for producing synthesis gas through biomass pyrolysis and gasification |
| CN103100357B (en) * | 2011-11-09 | 2016-08-10 | 新奥科技发展有限公司 | A kind of overflow mechanism and the fluidizing equipment with this device |
| CN102604683A (en) * | 2011-12-20 | 2012-07-25 | 新奥科技发展有限公司 | Method for co-production of synthetic gas and coal tar |
| CN106683734A (en) * | 2016-12-30 | 2017-05-17 | 浙江大学 | Method for processing waste resin by using dual-zone fluidized bed steam reforming device |
| CN108219851B (en) * | 2018-01-09 | 2021-01-05 | 新奥科技发展有限公司 | Coal gasification method and system |
| CN111854477B (en) * | 2019-04-28 | 2024-07-09 | 航天长征化学工程股份有限公司 | Cooling device |
| CN110776959A (en) * | 2019-11-08 | 2020-02-11 | 王树宽 | Integrated pyrolysis gasification device and method for seed coal |
| CN115725859B (en) * | 2022-11-21 | 2024-03-26 | 河南龙佰智能装备制造有限公司 | Titanium sponge fluidization reaction system and method |
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