CN102021038A - 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
- Publication number
- CN102021038A CN102021038A CN2009101703874A CN200910170387A CN102021038A CN 102021038 A CN102021038 A CN 102021038A CN 2009101703874 A CN2009101703874 A CN 2009101703874A CN 200910170387 A CN200910170387 A CN 200910170387A CN 102021038 A CN102021038 A CN 102021038A
- Authority
- CN
- China
- Prior art keywords
- space
- gas
- overflow device
- bed
- gas distributor
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Images
Landscapes
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
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 vapourizing furnace, specifically, the present invention relates to the multicompartment fluidized bed vapourizing furnace that methane-rich gas is produced in a kind of gasification of coal.
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 structure increases sharply.And that domestic Sweet natural gas still is in exploratory development is early stage, and import also is in the starting stage, and deliverability seriously lags behind, and causes the Sweet 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 can utilize existing natural gas line, and with lower economic cost, effectively alleviate the imbalance between supply and demand of Sweet natural gas, this is the effective measure that coal resources fully utilize.
Common gasification of coal system methane process, promptly coal at high temperature with oxygen (or air) and/or water vapor (H
2O) vaporized chemical of Zu Chenging carries out gasification reaction in the vapourizing furnace of individual layer, generates to contain a small amount of methane (CH
4) synthetic gas (mainly being hydrogen, carbon monoxide and carbonic acid gas), carry out hydrosphere transformation and methanation operation afterwards, adopt two-step approach to prepare methane.This coal process have the gasification reaction energy consumption big, to the equipment requirements height, and need three reaction units, technology than shortcomings such as complexity.
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 vapor (H with main component under relatively low temperature
2O), hydrogen (H
2), the gaseous mixture of carbon monoxide (CO) carries out gasification reaction under the katalysis of catalyzer, generate the methane (CH of high density
4).
At present, the methane technology for preparing the catalytic coal gasifaction of mentioning in the relevant patent adopts low temperature separation process that the methane in the aerogenesis is separated with carbon monoxide, hydrogen, hydrogen in the reactant gases and carbon monoxide are recycled in the vapourizing furnace, make it in vapourizing 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 finished in the vapourizing furnace of individual layer, but low, the long reaction time of gasification reaction speed, efficiency of carbon conversion is lower, and gas separation system is invested high shortcoming; For satisfying the thermally equilibrated needs of reactor, need to advance the stove superheated vapour and be heated to comparatively high temps, 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 conversion.The main fluidized-bed operating gas velocity is higher, and the part carbon granule is carried secretly to the secondary fluidized-bed, than carrying out gasification reaction under the low gas velocity, increases the solid phase residence time, improves efficiency of carbon conversion to greatest extent.Adopt multistage gasification carbon utilisation rate can 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, the facility investment height, operation is complicated.
United States Patent (USP) 4,094,650 mention under catalytic alkali metal, carbonaceous solids can be gasified, preparation methane, catalyzer need reclaim again and use.Reclaim water-soluble catalyst by multistage washing, lime slaking reclaims non-dissolubility catalyzer.United States Patent (USP) 0277437 is at United States Patent (USP) 4,094, on 650 bases, adopting one-level to handle separates the basic metal material from the reactor solids residue, simplified the base metal catalysts removal process, improved the economy and the total 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 single stage method system methane technology, 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 catalyzer carries out pre-mixing, enter the coal gasification furnace reactor, the superheated vapour that feeds is not only as vaporized chemical, simultaneously as thermal source, keep the reaction in furnace temperature, temperature is about 700 ℃ in the control stove, 850 ℃ of superheat steam temperatures, vapourizing furnace reaction pressure 3.5MPa, coal reacts with superheated vapour under the effect of catalyzer, directly obtains the product methane-rich gas.U.S. GPE company makes further research on the basis of EXXON Technology, United States Patent (USP) 20070000177A1 also discloses the technology of the direct methanation of coal, catalyzer is alkaline carbonate or alkali metal hydroxide, vaporized chemical is a water vapour, its major technique feature is except adding efficiently methanation catalyst, also added calcium oxide in the middle of the coal dust of reaction, the carbonic acid gas that the absorption reaction process produces, thus further improve the content of methane.Owing to add the catalyzer that promotes that methane generates, but high temperature is unfavorable for the generation of methane, temperature of reaction generally is controlled at about 700 ℃, speed of response is slow, the transformation efficiency of carbon is low, do not have outside heating system heat to be difficult to keep, and increased the catalyst recovery unit operation, 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 vapourizing furnace, wherein feed 900 ℃～950 ℃ high-temperature gas such as the gas heating coal dust after the fuel combustion, and gasification, pyrolysis institute heat requirement are provided, and produce coal gas.This fluidized-bed gasification furnace can be for vertical, also can be horizontally, is vaporized chemical with 700 ℃～800 ℃ superheated vapours, and cooling section feeds saturation steam, pneumatic charging.The residence time of this device for prolonging coal dust, favourable solid phase processing, heat energy utilization rate height, but the reaction volume utilization ratio in the vapourizing furnace is low, influences solid phase processing; Carbon 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 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 gasification of coal preparation of technology 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 gasification of coal technology to prepare the gasification installation that is rich in methane gas.
For achieving the above object, the multicompartment fluidized bed vapourizing furnace that the present invention provides a kind of gasification of coal to produce methane-rich gas in first aspect, this fluidized-bed gasification furnace comprises:
The vapourizing furnace housing, this housing has vertical longitudinal center line, and limits an internal space therein;
In the described internal space of described housing perpendicular to described longitudinal center line and at the two-layer at least gas distributor of arranging along the different heights place of described longitudinal center line that is well plate format, described two-layer at least gas distributor comprises first gas distributor and is positioned at second gas distributor of described first sparger below that described first gas distributor and described second sparger are divided into upward sheaf space, space, middle layer and lower layer space with the described internal space of described housing;
Be arranged at the feed(raw material)inlet on the top, side of described housing, the described sheaf space of going up is led in this feed(raw material)inlet, is used for raw material is imported the described sheaf space of going up, and the general flow direction of described raw material is along described longitudinal center line from top to bottom;
Be positioned at the lime-ash outlet of the bottom of described housing;
Be positioned near the gasification agent inlet that vaporized chemical enters that is used for the side of described lime-ash outlet of bottom of described housing, the general flow direction of described vaporized chemical is along described longitudinal center line from bottom to top;
Be positioned at the gas exit of described case top;
Connect first overflow device that is provided with the tubular form that is both ends open on described first gas distributor, connect second overflow device that is provided with the tubular form that is both ends open on described second gas distributor, described first overflow device and second overflow device are used to make described raw material along meander wire from top to bottom, flow to space, described middle layer from the described sheaf space of going up by described first overflow device, flow into described lower layer space by space, described middle layer by described second overflow device 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 described first overflow device and described second overflow device perpendicular to described longitudinal center line, descend to avoid material to lead directly to.
In a kind of preferred implementation of the present invention, the longitudinal middle part of described housing also is provided with the middle part opening for feed.
In a kind of preferred implementation of the present invention, vertical bottom of described housing also is provided with the underfeed mouth.
In a kind of preferred implementation of the present invention, also be provided with in described any space of going up in sheaf space, space, middle 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 device of arranging at least.
In a kind of preferred implementation of the present invention, in described housing, the below of described second gas distributor also is provided with the 3rd gas distributor.
In a kind of preferred implementation of the present invention, described the 3rd gas distributor is doline.
In a kind of preferred implementation of the present invention, the angle of described overflow device and horizontal direction is more than or equal to 30 °.
In a kind of preferred implementation of the present invention, the part that described overflow device upper end exceeds gas distributor is an overflow weir, and the height of this overflow weir is held the decision of material amount by solid phase process period and bed, calculates with following formula:
h＝4wt/[πD
2ρ(1-ε)]
The height of weir plate of h---certain layer, unit is m
This layer of w---solid particulate inlet amount, unit is kg/h
This layer of t---solid phase process period, 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 operational condition, unit is kg/m
3
ε-----porosity of this layer bed under operational 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 upflow tube between them and bed, calculates with following formula:
H＝H
1+h
1-h
2
Wherein
Distance between two adjacent gas distributors of H----, unit is m;
H
1The height of the upflow tube 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 upflow tube between two gas distributors, and unit is m.
In a second aspect of the present invention, the multicompartment fluidized bed vapourizing furnace that provides a kind of gasification of coal to produce methane-rich gas, this fluidized-bed gasification furnace comprises:
The vapourizing furnace housing, this housing has vertical longitudinal center line, and limits an internal space therein;
One deck of arranging perpendicular to described longitudinal center line in the described internal space of described housing is the gas distributor of well plate format, and described gas distributor is divided into upward sheaf space and lower layer space with the described internal space of described housing;
Be arranged at the feed(raw material)inlet on the top, side of described housing, the described sheaf space of going up is led in this feed(raw material)inlet, is used for raw material is imported the described sheaf space of going up, and the general flow direction of described raw material is along described longitudinal center line from top to bottom;
Be positioned at the lime-ash outlet of the bottom of described housing;
Be positioned near the gasification agent inlet that vaporized chemical enters that is used for the side of described lime-ash outlet of bottom of described housing, the general flow direction of described vaporized chemical is along described longitudinal center line from bottom to top;
Be positioned at the gas exit of described case top;
Connect the overflow device that is provided with the tubular form that is both ends open on the described gas distributor, described overflow device is used to make described raw material from top to bottom, flows to described lower layer space from the described sheaf space of going up by described overflow device.
Compare with the fluidized-bed gasification furnace (needing to be provided with two-layer at least gas distributor) that a first aspect of the present invention provides, the fluidized-bed gasification furnace that a second aspect of the present invention provides is minimum only to need to be provided with one deck gas distributor, is divided into sheaf space and lower layer space with the internal space with vapourizing furnace.
One or more features in the preferred feature of the fluidized-bed gasification furnace that provides according to a first aspect of the invention can be provided the fluidized-bed gasification furnace that provides according to a second aspect of the invention.
Use the technological process summary that equipment of the present invention adopts (withThe fluidized-bed gasification furnace that a 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 middle layer space B (catalytic gasification district); Raw coal adds from reactor top pyrolysis section, passes through sheaf space A on the multicompartment fluidized bed vapourizing furnace (partial thermal decomposition district) successively, middle 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 of process partial thermal decomposition enters the catalytic gasification district, and reactions such as catalytic gasification, methanation take place under the effect of catalyzer, generates methane, carbon monoxide, available gas composition and carbonic acid gas, a spot of hydrogen sulfide and ammonia etc. such as hydrogen.Fully the coal residue of reaction does not enter the residue gasification zone, gasification generates gases such as carbon monoxide, hydrogen, carbonic acid gas under the effect of oxygen and water vapor, and carbon monoxide, hydrogen enter epimere catalytic gasification district, methanation reaction takes place under the effect of catalyzer, increase system methane production, the high-temperature vapor of generation provides the part heat for the catalytic gasification district.Control residue gasification zone processing condition, realize the separation of ash, Jiao, catalyzer, the high-temperature lower part divided catalyst is gaseous form and enters 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 vapourizing furnace exit gas is through isothermal dust-filtering unit, and dust returns vapourizing furnace and carries out gasification reaction, and gas carries out gas-liquid separation through the gas-liquid cold separation unit, obtains semi coking tar and raw gas.Enter gas-cleaning installation afterwards, remove sour gas such as carbonic acid gas 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 as reaction times lime-ash carbon content long, that discharge;
(2) multilayer coupled gasification, sheaf space A on the multicompartment fluidized bed vapourizing furnace (partial thermal decomposition district) utilizes the surplus temperature of catalytic gasification aerogenesis to heat the fine coal that has just entered, 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 middle layer space B; Orlop C when feeding vaporized chemical, feeds a small amount of oxygen residual residue that gasifies, and by the heat that burning, gasification to residue provide catalytic gasification to need, provides hydrogen and CO to help the catalytic gasification reaction simultaneously;
(3) prepare methane with two-step approach and compare, this device integrates three reactors, realizes logistics coupling, heat coupling, and confession reaction heat reduces the energy consumption of superheated vapour, has solved the carbonaceous problem of residue; Prolong mean residence time, increased the gas production capacity, improved efficiency of carbon conversion.
(4) from whole process, utilize this multicompartment fluidized bed vapourizing furnace gasification preparation to be rich in methane gas, thermo-efficiency is higher, and 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 levels, reduce the catalyzer cost; Simultaneously can utilize the part trade waste, improve methane content as the catalyzer raw material.
Description of drawings
Fig. 1 is the structure iron of one embodiment of the present of invention;
Fig. 2, Fig. 3, Fig. 4 are respectively the structure iron of other each embodiment of the present invention.
Embodiment
Shown in each accompanying drawing, the multicompartment fluidized bed vapourizing furnace that a first aspect of the present invention provides a kind of gasification of coal to produce methane-rich gas, this fluidized-bed gasification furnace comprises:
In the described internal space of described housing 3 perpendicular to described longitudinal center line and at the two-layer at least gas distributor of arranging along the different heights place of described longitudinal center line 2 that is well plate format, described two-layer at least gas distributor 2 comprises first gas distributor and is positioned at second gas distributor of described first sparger below that described first gas distributor and described second sparger are divided into upward sheaf space A, middle layer space B and lower layer space C with the described internal space of described housing;
Be arranged at the feed(raw material)inlet 4 on the top, side of described housing, the described sheaf space A of going up is led in this feed(raw material)inlet, is used for raw material is imported the described sheaf space A of going up, and the general flow direction of described raw material is along described longitudinal center line from top to bottom;
Be positioned at the lime-ash outlet 7 of the bottom of described housing 3;
Be positioned near the gasification agent inlet that vaporized chemical enters that is used for the side of described lime-ash outlet 7 of bottom of described housing, the general flow direction of described vaporized chemical is along described longitudinal center line from bottom to top;
Be positioned at the gas exit at described housing 3 tops;
Connect first overflow device 1 that is provided with the tubular form that is both ends open on described first gas distributor, connect second overflow device 1 that is provided with the tubular form that is both ends open on described second gas distributor, described first overflow device and second overflow device are used to make described raw material along meander wire from top to bottom, flow to described middle layer space B from the described sheaf space A that goes up by described first overflow device, flow into described lower layer space C by described middle layer space B by described second overflow device 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 described first overflow device and described second overflow device perpendicular to described longitudinal center line, descend to avoid material to lead directly to.
In a kind of preferred implementation of the present invention, the longitudinal middle part of described housing also is provided with middle part opening for feed 4.
In a kind of preferred implementation of the present invention, vertical bottom of described 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 described any space of going up among sheaf space A, middle 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 device of arranging at least.
In a kind of preferred implementation of the present invention, in described housing, the below of described second gas distributor also is provided with the 3rd gas distributor.
In a kind of preferred implementation of the present invention, described the 3rd gas distributor is the doline (see figure 3).
In a kind of preferred implementation of the present invention, the angle of described overflow device and horizontal direction is more than or equal to 30 °.
The multicompartment fluidized bed vapourizing furnace (not shown) that a second aspect of the present invention provides a kind of gasification of coal to produce methane-rich gas, this fluidized-bed gasification furnace comprises:
The vapourizing furnace housing, this housing has vertical longitudinal center line, and limits an internal space therein;
One deck of arranging perpendicular to described longitudinal center line in the described internal space of described housing is the gas distributor of well plate format, and described gas distributor is divided into upward sheaf space and lower layer space with the described internal space of described housing;
Be arranged at the feed(raw material)inlet on the top, side of described housing, the described sheaf space of going up is led in this feed(raw material)inlet, is used for raw material is imported the described sheaf space of going up, and the general flow direction of described raw material is along described longitudinal center line from top to bottom;
Be positioned at the lime-ash outlet of the bottom of described housing;
Be positioned near the gasification agent inlet that vaporized chemical enters that is used for the side of described lime-ash outlet of bottom of described housing, the general flow direction of described vaporized chemical is along described longitudinal center line from bottom to top;
Be positioned at the gas exit of described case top;
Connect the overflow device that is provided with the tubular form that is both ends open on the described gas distributor, described overflow device is used to make described raw material from top to bottom, flows to described lower layer space from the described sheaf space of going up by described overflow device.
Compare with the fluidized-bed gasification furnace (needing to be provided with two-layer at least gas distributor) that a first aspect of the present invention provides, the fluidized-bed gasification furnace that a second aspect of the present invention provides is minimum only to need to be provided with one deck gas distributor, so that the vapourizing furnace internal space is divided into sheaf space and lower layer space.
One or more features in the preferred feature of the fluidized-bed gasification furnace that provides according to a first aspect of the invention can be provided the fluidized-bed gasification furnace that provides according to a second aspect of the invention.
Referring to Fig. 1, a first aspect of the present invention provides a kind of equipment for gasification, can be applied to the multicompartment fluidized bed gasification of coal produces in the high methane gas system, this equipment is the multicompartment fluidized bed vapourizing furnace, comprising: go up sheaf space A (partial thermal decomposition district), middle layer space B (catalytic gasification district), orlop C (residue gasification zone).
Raw coal is by the opening for feed 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 by 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 enters 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 mixture of catalysts enter vapourizing furnace catalytic gasification district by the opening for feed 4 of middle layer space B, and mix by the coal dust of upflow tube 1 from the partial thermal decomposition of last sheaf space A, with the reaction of vaporized chemical generating gasification, generate CH under the effect of catalyzer
4, CO, H
2Deng available gas composition and CO
2, a spot of H
2S and NH
3Deng.Principal reaction is as follows:
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 enter epimere middle layer space B (catalytic gasification district), methanation reaction takes place under the effect of catalyzer, increase system's methane production, the high-temperature vapor of Chan Shenging is middle layer space B (catalytic gasification district) in addition, and partial reaction institute heat requirement is provided.
Fully the coal residue of reaction does not enter the residue gasification zone, at O
2Generate CO, H with the following gasification of the effect of water vapor
2, CO
2Deng gas.Principal 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→CO2+H
2?(8)
CO, H that vapourizing furnace residue gasification zone C produces
2, can enter epimere middle layer space B (catalytic gasification district), methanation reaction takes place under the effect of catalyzer, increase system methane production, high-temperature gas of Chan Shenging and water vapour have reduced the lime-ash carbon content for the catalytic gasification district provides the part heat in addition, improve charging coal dust comprehensive utilization ratio.
Orlop C (residue gasification zone), temperature is higher, the part catalyzer evaporates into middle layer space B (catalytic gasification district) with gaseous form, recycling of fluidized-bed inner catalyst can reduce catalyzer addition in the initial coal dust, reduce the burden of catalyst recovery system, or need not to dispose in addition catalyst recovery system.
Vaporized chemical superheated vapour and minor amounts of oxygen enter the residue gasification zone from vapourizing furnace bottom, burn with residue, gasification reaction, and (catalytic gasification district) provides required heat for the middle layer space B.
Platoon slag equipment under the multicompartment fluidized bed vapourizing 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 vapourizing furnace produces is discharged by furnace roof, enters the later separation cleaning section.
Embodiment 1:
Referring to Fig. 2, on the basis of structure iron 1, as the heat that only depends on residue gasification to produce is difficult to satisfy the temperature required requirement of catalytic gasification, can establish an opening for feed 5 on the body of heater 3 of the orlop C of multicompartment fluidized bed, adds a small amount of raw coal to the residue gasification zone by this opening for feed.
Embodiment 2:
Referring to Fig. 3, on the basis of structure iron 1,, can change the grid distributor of multicompartment fluidized bed orlop C for satisfying the needs of ash discharge or process conditions, use the doline grid distributor, regulate and control ash discharge gas speed and fluidizing gas velocity respectively by inlet mouth 6,7.
Embodiment 3:
Referring to Fig. 4, on the basis of structure iron 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 upflow tube, as the plug formula upflow tube of band mechanical drive.Position by mechanical drive adjusting plug 8 changes gas direction and feed opening cross-sectional sizes, realizes smooth overflow.
Relative position about overflow device and gas distributor:
1. upflow tube can be installed in place, any horizontal 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 particulate to flow between two upflow tubes, the outlet of upper end upflow tube should maintain a certain distance in the horizontal direction with the import of lower end upflow tube, avoids distance too little (all being placed in the gas distributor center as two upflow tubes) as far as possible.
2. the height of overflow weir (the upflow tube upper end exceeds the part of gas distributor) is held the decision of material amount by solid phase process period and bed, calculates with following formula:
h＝4wt/[πD
2ρ(1-ε)]
H---layer of height of weir plate, unit is m
This layer of w---solid particulate inlet amount, unit is kg/h
This layer of t----solid phase process period, 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 operational condition, unit is kg/m
3
ε-----porosity of this layer bed under operational condition
3. the distance between two adjacent gas distributors is held the height decision of material amount by height that is in the upflow tube between them and bed, calculates with following formula:
H＝H
1+h
1-h
2
Wherein
Distance between two adjacent gas distributors of H----, unit is m;
H
1The height of the upflow tube 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 upflow tube between two gas distributors, and unit is m.
Core technology point of the present invention:
1, the integraty of multicompartment fluidized bed: vaporized chemical feeds from the vapourizing furnace bottom, and raw coal adds from reactor top pyrolysis section, successively last sheaf space A, middle 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
4Pyrolysis gas and product such as tar.Afterwards, reactions such as catalytic gasification, methanation take place in the middle layer space B (catalytic gasification district) that the coal dust of process partial thermal decomposition enters multicompartment fluidized bed under the effect of catalyzer, generate CH
4, CO, H
2Deng available gas composition and CO
2, a spot of H
2S and NH
3Deng.The coal residue that fully reacts does not enter the orlop C (residue gasification zone) of multicompartment fluidized bed, at O
2Generate CO, H with the following gasification of the effect of water vapor
2, CO
2Deng gas.
2, the tight association of multicompartment fluidized bed orlop C and middle 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 middle layer space B, the catalytic gasification section, required heat is provided, reduce the lime-ash carbon content, improve charging coal dust comprehensive utilization ratio; Simultaneously, at high temperature the part catalyzer evaporates into the middle layer space B (catalytic gasification district) of multicompartment fluidized bed with gaseous form, recycling of fluidized-bed inner catalyst can reduce catalyzer addition in the initial coal dust, reduce the burden of catalyst recovery system, or need not to dispose in addition catalyst recovery system; Vapourizing furnace residue gasification zone, multicompartment fluidized bed orlop C, the CO of generation, H
2, can enter multicompartment fluidized bed middle layer space B (catalytic gasification district), methanation reaction takes place under the effect of catalyzer, increase system's methane production, the high-temperature vapor of Chan Shenging provides the part heat for the catalytic gasification district in addition.
3, the selection of the opening for feed of multicompartment fluidized bed: according to the needs of system thermal balance and process conditions, except that the superiors' opening for feed of multicompartment fluidized bed, can be in the middle layer, the different positions place of orlop body of heater 3 sets up opening for feed.
4, the number of plies of multi-compartment bed: can be according to the needs of the residence time and process conditions, partial thermal decomposition district, catalytic gasification district, residue gasification zone with the multicompartment fluidized bed vapourizing furnace, be divided into single or multiple lift respectively, each interlayer separates with gas distributor 2, and overflow device 1 is installed.
5, overflow device 1: can be the mechanical type overflow device, as the lower end at upflow tube plug, valve are installed, can be the Pneumatic-control type overflow device also, as straight tube, and tapered tube, 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 grid distributor, tilt distribution plate or doline grid distributor, or their array configuration.The gas distributor 2 of multicompartment fluidized bed lower gas ingress can be dull and stereotyped grid distributor, tilt distribution plate, doline grid distributor, or band effusive gas distribution grid.
7, this multicompartment fluidized bed vapourizing 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 vapourizing furnace of methane gas, this vapourizing furnace is realized the continous-stable overflow of multicompartment fluidized bed interlayer by overflow device 1, pyrolysis, gasification, burning are coupled in the multicompartment fluidized bed, the realization classification transforms, with catalytic gasification system methane is that energy distribution is carried out at the center, 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) fluidized-bed, has prolonged the solid phase residence time, improves efficiency of carbon conversion to greatest extent, reduces facility investment, simultaneously easy handling;
Secondly, compare with the device in other patents, the gasification reaction of the residue gasification zone by multi-compartment bed orlop C provides hydrogen and carbon monoxide to the catalytic gasification district in middle layer, promote the carrying out of methanation reaction, need not separating hydrogen gas and CO (carbon monoxide converter) gas separation system, significantly reduce facility investment, simplify the operation; Simultaneously at multi-compartment bed orlop C, feed vaporized chemical and minor amounts of oxygen, the burning of part residue, catalytic gasification reaction to the middle layer space B provides reaction required part heat, both can reduce the import steam temperature, reduce steam superheating system and heat exchange system load, also solved the carbonaceous problem of residue.
In addition, the methane that sheaf space A pyrolysis section generates on the multi-compartment bed, the vapourizing 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 middle layer space B, have higher thermo-efficiency, also bring convenience for the postorder treatment system.
At last, with regard to the utilization of catalyzer, these multi-compartment bed the superiors generate restrain tar to change into and promote tar to generate, and reduce catalyst levels, reduce the catalyzer cost; Simultaneously can utilize the part trade waste, improve methane content as the catalyzer raw material.
Claims (15)
1. the multicompartment fluidized bed vapourizing furnace of methane-rich gas is produced in a gasification of coal, and this fluidized-bed gasification furnace comprises:
The vapourizing furnace housing, this housing has vertical longitudinal center line, and limits an internal space therein;
In the described internal space of described housing perpendicular to described longitudinal center line and at the two-layer at least gas distributor of arranging along the different heights place of described longitudinal center line that is well plate format, described two-layer at least gas distributor comprises first gas distributor and is positioned at second gas distributor of described first sparger below that described first gas distributor and described second sparger are divided into upward sheaf space, space, middle layer and lower layer space with the described internal space of described housing;
Be arranged at the feed(raw material)inlet on the top, side of described housing, the described sheaf space of going up is led in this feed(raw material)inlet, is used for raw material is imported the described sheaf space of going up, and the general flow direction of described raw material is along described longitudinal center line from top to bottom;
Be positioned at the lime-ash outlet of the bottom of described housing;
Be positioned near the gasification agent inlet that vaporized chemical enters that is used for the side of described lime-ash outlet of bottom of described housing, the general flow direction of described vaporized chemical is along described longitudinal center line from bottom to top;
Be positioned at the gas exit of described case top;
Connect first overflow device that is provided with the tubular form that is both ends open on described first gas distributor, connect second overflow device that is provided with the tubular form that is both ends open on described second gas distributor, described first overflow device and second overflow device are used to make described raw material along meander wire from top to bottom, flow to space, described middle layer from the described sheaf space of going up by described first overflow device, flow into described lower layer space by space, described middle layer by described second overflow device again.
2. fluidized-bed gasification furnace as claimed in claim 1 is characterized in that, is spaced from each other on the horizontal direction perpendicular to described longitudinal center line between the upper end of the lower end of described first overflow device and described second overflow device, 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 described housing also is provided with the middle part opening for feed.
4. fluidized-bed gasification furnace as claimed in claim 1 is characterized in that, vertical bottom of described 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 described any space of going up in sheaf space, space, middle 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 device of arranging at least.
6. fluidized-bed gasification furnace as claimed in claim 1 is characterized in that, in described housing, the below of described 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, described the 3rd gas distributor is doline.
8. as each described fluidized-bed gasification furnace of claim 1 to 7, it is characterized in that the angle of described overflow device and horizontal direction is more than or equal to 30 °.
9. as each described fluidized-bed gasification furnace of claim 1 to 7, it is characterized in that,
The part that described overflow device upper end exceeds gas distributor is an overflow weir, and the height of this overflow weir is held the decision of material amount by solid phase process period and bed, calculates with following formula:
h＝4wt/[πD
2ρ(1-ε)]
The height of weir plate of h---certain layer, unit is m;
This layer of w---solid particulate inlet amount, unit is kg/h;
This layer of t----solid phase process period, 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 operational condition, unit is kg/m
3
ε-----porosity of this layer bed under operational condition.
10. as 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 upflow tube between them and bed, calculates with following formula:
H＝H
1+h
1-h
2
Wherein
Distance between two adjacent gas distributors of H----, unit is m;
H
1The height of the upflow tube 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 upflow tube between two gas distributors, and unit is m.
11. the multicompartment fluidized bed vapourizing furnace of methane-rich gas is produced in a gasification of coal, this fluidized-bed gasification furnace comprises:
The vapourizing furnace housing, this housing has vertical longitudinal center line, and limits an internal space therein;
One deck of arranging perpendicular to described longitudinal center line in the described internal space of described housing is the gas distributor of well plate format, and described gas distributor is divided into upward sheaf space and lower layer space with the described internal space of described housing;
Be arranged at the feed(raw material)inlet on the top, side of described housing, the described sheaf space of going up is led in this feed(raw material)inlet, is used for raw material is imported the described sheaf space of going up, and the general flow direction of described raw material is along described longitudinal center line from top to bottom;
Be positioned at the lime-ash outlet of the bottom of described housing;
Be positioned near the gasification agent inlet that vaporized chemical enters that is used for the side of described lime-ash outlet of bottom of described housing, the general flow direction of described vaporized chemical is along described longitudinal center line from bottom to top;
Be positioned at the gas exit of described case top;
Connect the overflow device that is provided with the tubular form that is both ends open on the described gas distributor, described overflow device is used to make described raw material from top to bottom, flows to described lower layer space from the described sheaf space of going up by described overflow device.
12. fluidized-bed gasification furnace as claimed in claim 11 is characterized in that, the longitudinal middle part of described housing also is provided with the middle part opening for feed.
13. fluidized-bed gasification furnace as claimed in claim 11 is characterized in that, vertical bottom of described 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 described 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 device of arranging at least.
15., it is characterized in that the angle of described overflow device and horizontal direction is more than or equal to 30 ° as each described fluidized-bed gasification furnace of claim 11 to 14.
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| 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 |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200910170387 CN102021038B (en) | 2009-09-14 | 2009-09-14 | Multilayer fluidized bed gasification furnace for preparing methane-rich gas by coal gasification |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102021038A true CN102021038A (en) | 2011-04-20 |
| CN102021038B CN102021038B (en) | 2012-10-10 |
Family
ID=43862825
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 200910170387 Active CN102021038B (en) | 2009-09-14 | 2009-09-14 | Multilayer fluidized bed gasification furnace for preparing methane-rich gas by coal gasification |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102021038B (en) |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102329651A (en) * | 2011-08-26 | 2012-01-25 | 北京大学深圳研究生院 | Three-stage gasification device for producing synthesis gas through biomass pyrolysis and gasification |
| 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 |
| CN103100357A (en) * | 2011-11-09 | 2013-05-15 | 新奥科技发展有限公司 | Overflow device and fluidization equipment with the same |
| 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 |
| CN108219851A (en) * | 2018-01-09 | 2018-06-29 | 新奥科技发展有限公司 | A kind of coal gasification method and system |
| CN110776959A (en) * | 2019-11-08 | 2020-02-11 | 王树宽 | Integrated pyrolysis gasification device and method for seed coal |
| CN111854477A (en) * | 2019-04-28 | 2020-10-30 | 航天长征化学工程股份有限公司 | Cooling device |
| CN115725859A (en) * | 2022-11-21 | 2023-03-03 | 河南龙佰智能装备制造有限公司 | Titanium sponge fluidization reaction system and method |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3867110A (en) * | 1973-12-17 | 1975-02-18 | Inst Gas Technology | Method of coal pretreatment |
| DE3916325A1 (en) * | 1989-05-19 | 1990-11-22 | Grochowski Horst | WALKING BED REACTOR |
| US6955695B2 (en) * | 2002-03-05 | 2005-10-18 | Petro 2020, Llc | Conversion of petroleum residua to methane |
| CN101261010B (en) * | 2008-04-22 | 2011-06-08 | 青岛科技大学 | Double distribution plate coal-base serial fluidized-bed chemical chain combustion apparatus |
-
2009
- 2009-09-14 CN CN 200910170387 patent/CN102021038B/en active Active
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102329651A (en) * | 2011-08-26 | 2012-01-25 | 北京大学深圳研究生院 | Three-stage gasification device for producing synthesis gas through biomass pyrolysis and gasification |
| CN103100357A (en) * | 2011-11-09 | 2013-05-15 | 新奥科技发展有限公司 | Overflow device and fluidization equipment with the same |
| 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 |
| CN108219851A (en) * | 2018-01-09 | 2018-06-29 | 新奥科技发展有限公司 | A kind of coal gasification method and system |
| CN111854477A (en) * | 2019-04-28 | 2020-10-30 | 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 |
| CN115725859A (en) * | 2022-11-21 | 2023-03-03 | 河南龙佰智能装备制造有限公司 | Titanium sponge fluidization reaction system and method |
| 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 |
Also Published As
| Publication number | Publication date |
|---|---|
| CN102021038B (en) | 2012-10-10 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102021038B (en) | Multilayer fluidized bed gasification furnace for preparing methane-rich gas by coal gasification | |
| CN100361889C (en) | Secondary transformation technological method of high concentration carbon monooxide | |
| CN103923705B (en) | Gasifying biomass produces the device and method of hydrogen-rich gas | |
| CN103468322B (en) | A kind of method being produced hydrogen-rich gas by solid organic matters steam gasification | |
| CN102021037B (en) | Method and apparatus for preparing methane by catalytic gasification of coal | |
| WO2011029282A1 (en) | Method for preparing methane-containing gas through multi-region coal gasification and gasification furnace thereof | |
| CN202543155U (en) | Combined circulation system for gasified combustion and catalyst regeneration by adopting heat carrier as basis | |
| WO2011029285A1 (en) | Multi-layer fluidized bed gasifier | |
| CN106590761B (en) | Fluidized bed reaction device and reaction method for preparing methane-rich synthesis gas through catalytic coal gasification | |
| CN101817716B (en) | Method and device for catalyzing methanation of synthesis gas | |
| CN102796561B (en) | Anaerobic gasification method and device for biomass fuels by carbon dioxide circulation | |
| CN112607705B (en) | Steam methane reforming hydrogen production device and process | |
| CN102585947A (en) | Method and device for preparing methane-containing gas by using coal | |
| CN103571541B (en) | A kind of co-production of methane and the catalysis gasification method of tar | |
| CN106220461A (en) | A kind of device and method directly preparing methane based on coal chemistry chain gasification | |
| CN107760384B (en) | Efficient device and method for preparing methane-rich synthesis gas through catalytic coal gasification | |
| CN106590753A (en) | Gasification device for preparing methane-rich synthesis gas by coal and method of gasification reaction | |
| CN105176594A (en) | Device and method for producing reducing gas by lignite gasification | |
| CN104498117A (en) | Method and device for preparing methane-enriched gas from carbon-containing raw materials | |
| CN102399595B (en) | Multilayer fluidized bed gasification furnace | |
| CN103087778A (en) | Jet pipe, fluidized bed reactor with jet pipe and coal catalyzing and gasifying method | |
| CN105129800A (en) | Process and system of preparing calcium carbide and ethylene through oxygen/coal injection | |
| CN205035331U (en) | A device that is used for brown coal gasification system reducing gas | |
| CN104987891B (en) | A kind of alternative fuel based on coal hydrocarbon component classification gasification/chemical products production system | |
| CN211111863U (en) | Biomass oil-gas co-production device based on chemical chain |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |