CN107513437A - A kind of Horizontal type circulating fluid bed gasification process and device - Google Patents
A kind of Horizontal type circulating fluid bed gasification process and device Download PDFInfo
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- CN107513437A CN107513437A CN201710955126.8A CN201710955126A CN107513437A CN 107513437 A CN107513437 A CN 107513437A CN 201710955126 A CN201710955126 A CN 201710955126A CN 107513437 A CN107513437 A CN 107513437A
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- 238000002309 gasification Methods 0.000 title claims abstract description 116
- 238000000034 method Methods 0.000 title claims abstract description 23
- 239000012530 fluid Substances 0.000 title claims abstract description 21
- 230000008569 process Effects 0.000 title claims abstract description 12
- 239000006200 vaporizer Substances 0.000 claims abstract description 119
- 239000003034 coal gas Substances 0.000 claims abstract description 37
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 31
- 239000007787 solid Substances 0.000 claims abstract description 29
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 24
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 23
- 239000000463 material Substances 0.000 claims abstract description 22
- 239000011343 solid material Substances 0.000 claims abstract description 14
- 238000000926 separation method Methods 0.000 claims abstract description 13
- 239000000446 fuel Substances 0.000 claims abstract description 12
- 238000000605 extraction Methods 0.000 claims abstract description 8
- 239000007789 gas Substances 0.000 claims description 46
- 230000004927 fusion Effects 0.000 claims description 13
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 12
- 229910052760 oxygen Inorganic materials 0.000 claims description 12
- 239000001301 oxygen Substances 0.000 claims description 12
- 238000009434 installation Methods 0.000 claims description 10
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims description 5
- 230000003134 recirculating effect Effects 0.000 claims description 5
- 238000002156 mixing Methods 0.000 claims description 2
- 239000000428 dust Substances 0.000 abstract description 26
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 abstract description 19
- 229910052698 phosphorus Inorganic materials 0.000 abstract description 19
- 239000011574 phosphorus Substances 0.000 abstract description 19
- 239000002893 slag Substances 0.000 abstract description 13
- 238000006243 chemical reaction Methods 0.000 abstract description 10
- 239000003500 flue dust Substances 0.000 abstract description 7
- 238000005516 engineering process Methods 0.000 abstract description 4
- 239000002956 ash Substances 0.000 description 29
- 239000003245 coal Substances 0.000 description 24
- 239000000843 powder Substances 0.000 description 8
- 238000002485 combustion reaction Methods 0.000 description 6
- 239000000203 mixture Substances 0.000 description 4
- 239000002245 particle Substances 0.000 description 4
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 3
- 239000010882 bottom ash Substances 0.000 description 3
- 230000008859 change Effects 0.000 description 3
- 239000002817 coal dust Substances 0.000 description 3
- 239000003546 flue gas Substances 0.000 description 3
- 230000008018 melting Effects 0.000 description 3
- 238000002844 melting Methods 0.000 description 3
- 230000008901 benefit Effects 0.000 description 2
- 239000000567 combustion gas Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000005243 fluidization Methods 0.000 description 2
- 239000010881 fly ash Substances 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 230000036632 reaction speed Effects 0.000 description 2
- 239000002028 Biomass Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000004566 building material Substances 0.000 description 1
- 239000000919 ceramic Substances 0.000 description 1
- 239000000839 emulsion Substances 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000155 melt Substances 0.000 description 1
- 230000005855 radiation Effects 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000009257 reactivity Effects 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
- C10J3/56—Apparatus; Plants
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
- C10J3/721—Multistage gasification, e.g. plural parallel or serial gasification stages
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
- C10J3/725—Redox processes
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
- C10J3/82—Gas withdrawal means
- C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0953—Gasifying agents
- C10J2300/0956—Air or oxygen enriched air
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0953—Gasifying agents
- C10J2300/0959—Oxygen
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0953—Gasifying agents
- C10J2300/0973—Water
- C10J2300/0976—Water as steam
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
- C10J2300/1603—Integration of gasification processes with another plant or parts within the plant with gas treatment
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The present invention provides a kind of Horizontal type circulating fluid bed gasification process and device, is related to solid carbonaceous fuels gasification technology field.Methods described is gasified using subregion, add the solid carbonaceous fuels in the first vaporizer and carry out gasification reaction generation raw gas with the first gasifying agent in the first vaporizer, raw gas is transported to the second vaporizer, and unreacted carbonaceous solids material and coal gas are isolated by inertia separator；The carbonaceous solids material falls into the second vaporizer, with the second gasifying agent in the second vaporizer, with compared with further gasification produces coal gas under higher gasification temperature in the first vaporizer, the coal gas mixes with the coal gas from the first vaporizer isolated through inertia separator, form the mixed gas containing solid material, purified gas output is formed after cyclonic separation again, the solid material of separation returns to the first vaporizer through feeding back device；First vaporizer bottom dry ash extraction.Described device mainly includes the first vaporizer, the second vaporizer, inertia separator, cyclone separator, standpipe, material returning device etc..This method overcomes phosphorus content in existing circle fluidized-bed gasification furnace solid slag with device and, compared with the problem of flying dust amount is big, unburned carbon in flue dust is high in high, coal gas, improves efficiency of carbon con version and cold gas efficiency, more effectively utilize solid carbonaceous fuels.
Description
Technical field
The present invention relates to solid carbonaceous fuels gasification technology field；Relate in particular to a kind of Horizontal type circulating fluid bed gasification
Method and apparatus, belong to the combustion gas of solid carbonaceous fuels vaporizing system or synthesis gas technical field under fluidization.
Background technology
Chinese invention patent 201410117504.1, applying date 2014.3.26, publication date 2014.7.9, publication number
CN103911179A, title：Coal gasification method and device；It discloses the circle fluidized-bed gasification furnace of existing dry ash extraction
Phosphorus content in solid slag is compared with the problem of flying dust amount is big, phosphorus content is high in high, coal gas.And Chinese invention patent application
201510641319.7, applying date 2015.9.30, publication date 2017.4.5, publication number CN106554826A, title：Band fine powder
The circulation fluidized bed coal gasifying method and device of ash melting；It discloses the gasification of existing recirculating fluidized bed due to gasification operation temperature
Spend low, cause that phosphorus content in the fine ash that is entrained with air-flow is high, and mass fraction accounts for 30%~50%, and flying dust accounts for total ash quantity 70%
~80% causes total carbon utilisation rate of system not high；And the disposal that utilizes of wherein fine ash is also a great problem.
In traditional circle fluidized-bed gasification furnace, because by the way of dry ash extraction, coal gasification temperature is relatively low, typically
Less than 150~200 DEG C of ash fusion point.Influenceed by the reactivity and ash fusion point of coal, the gas of general circulation fluidized bed coal gasifying stove
Change temperature and elect 950 DEG C~1050 DEG C or so as.The particle diameter for the as-fired coal powder that circulation fluidized bed coal gasifying stove uses is generally in 10mm
Below left and right, after coal dust enters the burner hearth of circulation fluidized bed coal gasifying stove, quickly mix with high temperature circulation bed, quickly added
Heat, rapid evaporation, the fast pyrogenation reaction of moisture occurs, in this process, by the heat endurance and mechanically stable of coal dust
Property influence, part coal dust can crush, and produce small particle semicoke, or even fine powder semicoke.Semicoke is anti-with gasifying agent in riser
Should, coal gas is produced, the complete semicoke of unreacted enters cyclone separator, after most of semicoke is trapped by whirlwind, by standpipe and returns
Glassware, return to riser and continue to react with gasifying agent, remaining small part semicoke escapes out with coal gas of high temperature, turns into flying dust.
The flying dust amount of general recirculating fluidized bed is greatly and phosphorus content is high in flying dust, and general more than 20%, some coal seed gasifications
Phosphorus content is even up to 70% in flying dust.Phosphorus content is high in flying dust, on the one hand to the efficiency of carbon con version of circulation fluidized bed coal gasifying stove
Important negative effect is caused with cold gas efficiency etc., even resulting in efficiency of carbon con version reduces by 10% or so, and some coals even reach
18% or so, gas yield and system thermal efficiency significantly reduce.On the other hand, the high carbon content in flying dust, burning and gasification are lived
Property is low, is unfavorable for the direct utilization of flying dust.
Using Secondary Air mode, upper temp is high, available for gasifying, but O in Secondary Air2Can preferentially and gas-fired,
Produce CO2、H2O, the CO produced herein2Very slow with C gasification reaction speed, unlike being generated in bottom, the residence time is relatively
It is long.
It is general using to escape to high ash quantity, the processing of high carbon content flying dust in some circulation fluidized bed coal gasifying technologies
The flying dust for going out the cyclone separator of circle fluidized-bed gasification furnace is handled using two methods of burning, gasification, rather than directly
Strengthen the reaction in gasification furnace, reduce the carbon content in flying dust.
Raw gas is by again as caused by the use of Chinese invention patent 201410117504.1 by circle fluidized-bed gasification furnace
After one cyclonic separation, the flying dust of separation produces high-temperature flue gas by Combustion of Hot Air Furnace, send circle fluidized-bed gasification furnace as heat
Source, this process have been mixed into relatively large N2, dilute coal gas, calorific value of gas reduces, in addition the temperature of combustion product gases be up to 1300~
1400 DEG C, and hot-blast stove uses slag tap, therefore liquid slag drop can be mixed with the high-temperature flue gas of input gasification furnace, in gasification furnace
It is interior to be bonded with bed, reunite, destroy flowing.
Chinese invention patent 01123960.3, applying date 2001.8.8, publication date 2003.3.5, publication number CN1400289,
Title：Powdered coal fluidized bed gasification method and gasification furnace；It discloses the gasification of single burner hearth (to divide high temperature combustion zone+emulsion zone+dilute phase
Area), grey reunion deslagging, gasify ash+single hop fine powder coal-char combustion, and flue gas enters high temperature combustion zone.
Chinese invention patent 201610644936.7, applying date 2016.8.8, publication date 2016.11.16, publication number
CN106118750A, title:Step combines bed gasification system；It is (high it discloses+two sections of entrained flow gasifications of one section of fluidized gasification
Temperature), slag tap, single hop deslagging, gasification ash.But two sections of gasifying agents are oxygen or oxygen-enriched air.
Chinese invention patent 201110431593.3, applying date 2011.12.14, publication date 2012.7.4, publication number
CN102533345A, title：The method and device of coal gasification in combined type fluidized bed；It discloses a kind of ash to melt gather qi together+fine powder
Semicoke entrained flow gasification (dry ash extraction)+coal gas of high temperature enters gasification furnace.It uses+two sections of entrained flow gasifications of one section of fluidized gasification
(1100~1300 DEG C), single hop deslagging, ash melts poly- deslagging；The raw material of two sections of gasification furnaces is flying dust, comes from two level cyclonic separation
Device, heating gas radiation waste heat recovery boiler, coal gas ceramic filter, rather than it is primary cyclone, high circulation multiplying power
Fine powder semicoke；The fine slag of air flow bed enters gasification furnace with coal gas of high temperature；Oxygen is needed to improve efficiency of carbon con version, production as gasifying agent
Coal gas of high temperature；To low-ash-fusion coal, or air flow bed produces liquid slag, then cool down, the flowing destroyed in fluidized-bed gasification furnace, or
Gasification temperature need to be reduced, efficiency is low.After the gasification of fluidized-bed gasification furnace bottom is stable, by fine powder by fine powder charging transfer pot conveying
Oxygen and steam are passed through to air flow bed burner noz(zle), then to burner noz(zle), by oxygen dry pulverized coal than 0.5~0.7Nm3/kg, steam
Coal is operated than 0.1~0.3kg/kg, fluid bed of the air flow bed operation temperature in 1100~1300 DEG C of scopes, fluid bed with
Air flow bed crosses section temperature in 1050~1150 DEG C of scopes；
Chinese utility model patent 201520571134.9, applying date 2015.8.3, publication date 2016.3.2, publication number
CN205061998U, title：A kind of fine coal circulating energy-saving gasification furnace；It is disclosed that a kind of equipment, is gasified using single hop burner hearth,
Fly ash emission removes flying dust boiler combustion producing steam；More than 600 DEG C of high temperature air temperature, coordinate saturated vapor as gasifying agent.
Chinese invention patent application number 201510641319.7, applying date 2015.9.3, publication date 2017.4.5, publication number
CN106554826A, title：Circulation fluidized bed coal gasifying method and device with fine ash melting；It discloses a kind of equipment,
Using conventional CFB coal gasifications+fusing fly ash gasification, dry ash extraction+slag tap；From the flying dust (particle diameter of cyclone separator loss
20~40 μm, it is carbon containing it is high, flow rate is big) be collected into, then gasify through the preheating of fuel preheating section, high-temperature fusion section；Two sections of coal gas return
Send CFB gasification hearths.Using grey melting method gasification flying dust, then the concurrent heating of gasification furnace top is returned, shortcoming is slag tap, and flying dust is grey
Divide content high (such as 50%~70%), high energy consumption, and it is aerobic.
These existing circle fluidized-bed gasification furnaces all there is phosphorus content in solid slag it is big compared with flying dust amount in high, coal gas,
The problem of phosphorus content is high.
The content of the invention
For circle fluidized-bed gasification furnace present in prior art all there is phosphorus content in solid slag is higher, in coal gas
The problem of flying dust amount is big, unburned carbon in flue dust is high, technical problems to be solved of the embodiment of the present invention are to propose that a kind of effect is more preferable
Horizontal type circulating fluid bed gasification process and device.
In order to solve the above problems, the embodiment of the present invention proposes a kind of gasification process of recirculating fluidized bed, including：
Solid carbonaceous fuels are added into the first vaporizer, produced slightly with the gasification of the first gasifying agent in first vaporizer
Coal gas, the raw gas are transported to the second vaporizer, and unreacted carbonaceous solids material and coal are isolated in inertia separator
Gas；Carbonaceous solids material falls into second vaporizer, with the second gasifying agent in second vaporizer, with more described first
Further gasification produces coal gas under the higher gasification temperature of vaporizer, and gasification rate is with gasification temperature in power exponent increase；It is described
Coal gas mixes with the coal gas isolated through the inertia separator, forms the mixed gas containing solid material, the mixing
Coal gas forms purified gas output after cyclonic separation, and the solid material of separation returns to first gasification through feeding back device
Room.
Wherein, first gasifying agent and the second gasifying agent are respectively air, or the mixed gas of air, steam, or
The mixed gas of person's oxygen-enriched air, steam, or the mixed gas of pure oxygen, steam.
Wherein, wherein the temperature of the air preheated, oxygen-enriched air or pure oxygen is 200-850 DEG C, the pressure position of superheated steam
0.6-9.8MPa, temperature are 200-600 DEG C.
Wherein, the running temperature of first vaporizer is 900-1100 DEG C；The running temperature of second vaporizer is 1000-
1200℃。
Meanwhile in order to solve the above problems, the embodiment of the present invention also proposed a kind of Horizontal type circulating fluid bed gasification installation,
Mainly include the first vaporizer, the second vaporizer, inertia separator, cyclone separator, standpipe, material returning device, first gasification
Room is connected with second vaporizer by the inertia separator, forms " N " font air flue；First vaporizer with it is described
Coal gas caused by second vaporizer mixes in second vaporizer, separates to form purified gas output through cyclone separator, point
From the solid material return to first vaporizer through feeding back device；The bottom of first vaporizer is provided with the first gasification
Agent entrance；The bottom of second vaporizer is provided with the second gasification agent inlet.
Wherein, the gasification temperature in second vaporizer is higher than the gasification temperature of first vaporizer 50~150 DEG C.
Wherein, the gasification temperature in second vaporizer is less than 50~100 DEG C of ash fusion point.
Wherein, coal gas of first vaporizer after inertia separator separates enters in the reducing zone of second vaporizer
Enter second vaporizer.
Wherein, the first vaporizer bottom, which is provided with, is used for the slag-drip opening that solid-state claps residence.
Wherein, the feeding back device includes standpipe and material returning device, bottom and institute of the standpipe with the cyclone separator
State material returning device connection.
Wherein, the material returning device connects the first vaporizer by the connecting tube tilted down.
The above-mentioned technical proposal of the present invention has the beneficial effect that：Above-mentioned technical proposal proposes a kind of horizontal circulation fluidisation
Bed gasification method and device, which overcome that phosphorus content in the existing circle fluidized-bed gasification furnace solid slag used is higher, in coal gas
The problem of flying dust amount is big, phosphorus content is high, efficiency of carbon con version and cold gas efficiency are improved, bottom ash, flying dust, which can directly do building materials etc., to be made
With more effectively utilizing solid carbonaceous fuels.
Brief description of the drawings
Fig. 1 is the Horizontal type circulating fluid bed gasification installation structural representation of the embodiment of the present invention；
Description of reference numerals：
1：First vaporizer；
2：Second vaporizer；
3：Inertia separator；
4：Cyclone separator；
5：Standpipe；
6：Material returning device；
7：Returning charge wind entrance；
8：Purified gas exports；
A：Coal gas from the first vaporizer is segregated into the passage of the second vaporizer through inertia separator；
B：The reducing zone of second vaporizer；
C：Raw gas containing unreacted carbonaceous solids material caused by first vaporizer；
D：First vaporizer, the second mixed mixed gas of vaporizer coal gas；
G1：First gasifying agent；
G2：Second gasifying agent；
W:Dry ash extraction；
X：Solid carbonaceous fuels.
Embodiment
To make the technical problem to be solved in the present invention, technical scheme and advantage clearer, below in conjunction with accompanying drawing and tool
Body embodiment is described in detail.
The embodiment of the present invention proposes a kind of Horizontal type circulating fluid bed gasification process and device, and it uses the skill that subregion gasifies
Art.Because the dust burdening of solid bed in the first vaporizer is higher, the gasification temperature of the vaporizer of adjustment control first and conventional stream
Change the temperature close (as being less than 150~200 DEG C of ash fusion point) of bed gasification furnace, avoid that slagging phenomenon occurs, in the first vaporizer
Bottom deslagging, solid deslagging；The solid material of second vaporizer is containing with raw gas entrainment caused by the gasification of the first vaporizer
Carbon solid material, compared with the solid material in the first vaporizer, phosphorus content is higher, dust burdening is relatively low, particle diameter is thinner；Utilize height
The characteristics of carbon content, higher ash fusion point of low ash content semicoke, properly increases the gasification temperature of the second vaporizer, to strengthen gasification
Speed, the intensity of gasification, the phosphorus content for reducing flying dust and flow rate, the phosphorus content for reducing bottom ash.
Specifically, as shown in Figure 1, the Horizontal type circulating fluid bed gasification installation of the embodiment of the present invention, mainly include：First
Vaporizer 1, the second vaporizer 2, inertia separator 3, cyclone separator 4, standpipe 5, material returning device 6, returning charge wind inlet 7, purified gas
Outlet 8；The top of wherein described first vaporizer 1 connects with the inertia separator 2；The inertia separator 3 and described the
Two vaporizers 2 are connected by bottom gas passage A, form " N " font air flue；Second vaporizer 2 connects with cyclone separator 4
Logical, the top of cyclone separator 4 is provided with gas port 8, and the bottom of cyclone separator 4 connects with standpipe 5, and material returning device 6 is respectively with standing
Pipe 5 connects with the first vaporizer 1；Wherein, the bottom of first vaporizer 1 is provided with the first gasification agent inlet G1 and dry ash extraction
Mouth W；The bottom of second vaporizer 2 is provided with the second gasification agent inlet G2；First vaporizer 1 feeds provided with solid carbonaceous fuels
Mouth X, solid carbonaceous fuels are with the first gasifying agent gasification generation raw gas in the first vaporizer 1, and the raw gas C is by first
The top of vaporizer 1 reaches inertia separator 3, and raw gas C is separated into coal gas and the complete carbonaceous solids material of unreacted, and this is carbon containing solid
Body material falls into the bottom of the second vaporizer 2, and the coal gas is after the gas passage A of the second vaporizer 2 into the second vaporizer
Reducing zone B；The complete carbonaceous solids material of unreacted in the second vaporizer 2 with the second gasifying agent in compared with the first vaporizer 1 more
High gasification temperature issues raw gasification reaction and produces coal gas；Coal gas is in the second gas caused by first vaporizer 1, the second vaporizer 2
Change in room 2 and be mixed into the mixed gas containing solid material；Mixed gas passes through 8 outputs after the separation of cyclone separator 4.
Embodiment 1, using ash fusion point (ST), the gasification temperature of the first vaporizer is 900 DEG C, the second gas for 1100 DEG C of coal
The running temperature for changing room is 1000 DEG C, and gasifying agent is preheated air, and preheated air temperature is 600 DEG C.First vaporizer deslagging contains
Carbon amounts is 5%, and the unburned carbon in flue dust for going out the second cyclone separator is reduced to less than 13%.
Embodiment 2, ash fusion point (ST) is used as 1200 DEG C of coal, the gasification temperature of the first vaporizer is 1100 DEG C, second
The running temperature of vaporizer is 1150 DEG C, and gasifying agent is the mixture of preheated air and superheated steam, preheated air temperature 850
DEG C, superheated steam pressure, temperature be respectively 9.8MPa, 600 DEG C.First vaporizer deslagging phosphorus content is 4%, unburned carbon in flue dust drop
It is low to 8%.
Embodiment 3, ash fusion point (ST) is used as 1250 DEG C of coal, the gasification temperature of the first vaporizer is 1050 DEG C, second
The running temperature of vaporizer is 1200 DEG C, and gasifying agent is the mixture of oxygen-enriched air and superheated steam, and oxygen-enriched air temperature is 200
DEG C, superheat steam temperature 0.6MPa, 200 DEG C.First vaporizer deslagging phosphorus content is 4.5%, and unburned carbon in flue dust is reduced to
9.7%.
Embodiment 4, using ash fusion point (ST), the gasification temperature of the first vaporizer is 980 DEG C, the second gas for 1130 DEG C of coal
The running temperature for changing room is 1050 DEG C, and gasifying agent is the mixture of pure oxygen and superheated steam, and superheated steam pressure, temperature are respectively
4.5MPa, temperature are 450 DEG C.First vaporizer deslagging phosphorus content is 4%, and unburned carbon in flue dust is reduced to about 10%.
Embodiment 5, using ash fusion point (ST), the gasification temperature of the first vaporizer is 900 DEG C for 1050 DEG C of biomass, the
The running temperature of two vaporizers is 1000 DEG C, and gasifying agent is preheated air, and preheated air temperature is 230 DEG C.First vaporizer is arranged
Slag phosphorus content is 4.3%, and the unburned carbon in flue dust for going out the second cyclone separator is reduced to about 7.8%.
The Horizontal type circulating fluid bed gasification installation of the embodiment of the present invention has the advantage that：
(1) burner hearth of existing recirculating fluidized bed is divided into two vaporizers (the first vaporizer 1, the second vaporizer 2) and one
Individual inertia separation chamber 3, raw gas caused by the first vaporizer 1 is after the separation of inertia separator 3, in the reduction of the second vaporizer 2
Area enters the second vaporizer, therefore raw gas caused by the first vaporizer 1 will not be by the oxygen in the gasifying agent of the second vaporizer 2
Burn；
(2) it is limited to ash fusion point (especially softening temperature ST) and existing circle fluidized-bed gasification furnace bottom ash content is high
Feature, gasification temperature general control is at about 150~200 DEG C lower than ST.The present invention, by the mainly high gasification containing grey solid material
The second vaporizer 2 that first vaporizer 1 gasifies with mainly low ash content, high-carbon content solid material separates, respectively control fortune
Gasification temperature, and the vaporizer 1 of the second vaporizer 2 to the first uses higher gasification temperature, so can not only improve second
Gasification reaction speed in vaporizer 2, and then the intensity of gasification of the whole gasification furnace of raising, efficiency of carbon con version, cold gas efficiency etc., and
And the second not slagging in vaporizer.
Described above is the preferred embodiment of the present invention, it is noted that for those skilled in the art
For, on the premise of principle of the present invention is not departed from, some improvements and modifications can also be made, these improvements and modifications
It should be regarded as protection scope of the present invention.
Claims (10)
- A kind of 1. gasification process of Horizontal type circulating fluid bed, it is characterised in that including：Solid carbonaceous fuels add the first vaporizer, and gasifying in first vaporizer with the first gasifying agent produces raw gas, The raw gas is transported to the second vaporizer, and unreacted carbonaceous solids material and coal gas are isolated in inertia separator；Contain Carbon solid matter falls into second vaporizer, with the second gasifying agent in second vaporizer, with the more described first gasification Further gasification produces coal gas under the higher gasification temperature in room, and coal gas caused by the second vaporizer through the inertia separator with dividing The coal gas mixing separated out, forms the mixed gas containing solid material；Mixed gas forms purified gas and solid after cyclonic separation Material, then purified gas is exported, and the solid material is returned into first vaporizer through feeding back device.
- 2. the gasification process of Horizontal type circulating fluid bed according to claim 1, it is characterised in that first gasifying agent and Second gasifying agent is respectively air, either air, the mixed gas of steam or oxygen-enriched air, the mixed gas of steam, or The mixed gas of pure oxygen, steam.
- 3. the gasification process of Horizontal type circulating fluid bed according to claim 2, it is characterised in that the air that wherein preheats, The temperature of oxygen-enriched air or pure oxygen is 200-850 DEG C, and the pressure of superheated steam is 0.6-2.5MPa, and temperature is 200-600 DEG C.
- 4. the gasification process of recirculating fluidized bed according to claim 1, it is characterised in that the operation of first vaporizer Temperature is 900-1100 DEG C；The running temperature of second vaporizer is 1000-1200 DEG C.
- A kind of 5. Horizontal type circulating fluid bed gasification installation, it is characterised in that：Mainly include the first vaporizer, the second vaporizer, be used to Property separator, cyclone separator, standpipe, material returning device, first vaporizer and second vaporizer pass through the inertia point Connected from device, form " N " font air flue；Coal gas of first vaporizer after inertia separator separates and the described second gasification Coal gas caused by room mixes in second vaporizer, separated through cyclone separator to be formed purified gas output, separation it is described Solid material returns to first vaporizer through feeding back device；The bottom of first vaporizer is provided with the first gasification agent inlet； The bottom of second vaporizer is provided with the second gasification agent inlet.
- 6. Horizontal type circulating fluid bed gasification installation according to claim 5, it is characterised in that in second vaporizer Gasification temperature is higher than the gasification temperature of first vaporizer 50~150 DEG C.
- 7. Horizontal type circulating fluid bed gasification installation according to claim 5, it is characterised in that in second vaporizer Gasification temperature is less than 50~100 DEG C of ash fusion point.
- 8. Horizontal type circulating fluid bed gasification installation according to claim 5, it is characterised in that first vaporizer is through used Property separator separation after coal gas enter second vaporizer in the reducing zone of second vaporizer.
- 9. Horizontal type circulating fluid bed gasification installation according to claim 5, it is characterised in that the first vaporizer bottom Provided with the slag-drip opening for dry ash extraction.
- 10. Horizontal type circulating fluid bed gasification installation according to claim 5, it is characterised in that the feeding back device includes Standpipe and material returning device, the standpipe connect with the bottom of the cyclone separator and the material returning device, the material returning device pass through to Under inclined connecting tube connect the first vaporizer.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110628463A (en) * | 2019-10-28 | 2019-12-31 | 安徽科达洁能股份有限公司 | Mixed air distribution system of gas producer and working method |
| CN111349473A (en) * | 2018-12-24 | 2020-06-30 | 浙江科技学院 | Coal gasification furnace of circulating fluidized bed |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2008088310A (en) * | 2006-10-03 | 2008-04-17 | Kenji Yamane | High temperature carbonization method and high temperature carbonization apparatus |
| CN101691501A (en) * | 2009-09-30 | 2010-04-07 | 浙江大学 | Coal-grading conversion poly-generation device and method for producing coal gas, tar and carbocoal on circulating fluid bed |
| CN103836617A (en) * | 2014-02-28 | 2014-06-04 | 北京热华能源科技有限公司 | Horizontal circulating fluidized bed boiler with down-exhaust cyclone separator |
| CN105112105A (en) * | 2015-09-02 | 2015-12-02 | 上海尧兴投资管理有限公司 | Gasification coupled system and application thereof |
| CN207435396U (en) * | 2017-10-13 | 2018-06-01 | 国科洁能（北京）科技有限公司 | A kind of Horizontal type circulating fluid bed gasification installation |
-
2017
- 2017-10-13 CN CN201710955126.8A patent/CN107513437A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2008088310A (en) * | 2006-10-03 | 2008-04-17 | Kenji Yamane | High temperature carbonization method and high temperature carbonization apparatus |
| CN101691501A (en) * | 2009-09-30 | 2010-04-07 | 浙江大学 | Coal-grading conversion poly-generation device and method for producing coal gas, tar and carbocoal on circulating fluid bed |
| CN103836617A (en) * | 2014-02-28 | 2014-06-04 | 北京热华能源科技有限公司 | Horizontal circulating fluidized bed boiler with down-exhaust cyclone separator |
| CN105112105A (en) * | 2015-09-02 | 2015-12-02 | 上海尧兴投资管理有限公司 | Gasification coupled system and application thereof |
| CN207435396U (en) * | 2017-10-13 | 2018-06-01 | 国科洁能（北京）科技有限公司 | A kind of Horizontal type circulating fluid bed gasification installation |
Non-Patent Citations (1)
| Title |
|---|
| 周静,周志杰,王少云,龚欣,于遵宏: "含气化剂煤气深度气化研究" * |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111349473A (en) * | 2018-12-24 | 2020-06-30 | 浙江科技学院 | Coal gasification furnace of circulating fluidized bed |
| CN110628463A (en) * | 2019-10-28 | 2019-12-31 | 安徽科达洁能股份有限公司 | Mixed air distribution system of gas producer and working method |
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Application publication date: 20171226 |