CN203794844U - Indirect gasification system for biomass double fluidized beds - Google Patents
Indirect gasification system for biomass double fluidized beds Download PDFInfo
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- CN203794844U CN203794844U CN201420183701.9U CN201420183701U CN203794844U CN 203794844 U CN203794844 U CN 203794844U CN 201420183701 U CN201420183701 U CN 201420183701U CN 203794844 U CN203794844 U CN 203794844U
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- 238000002309 gasification Methods 0.000 title claims abstract description 56
- 239000002028 Biomass Substances 0.000 title claims abstract description 54
- 239000000463 material Substances 0.000 claims abstract description 86
- 239000007787 solid Substances 0.000 claims abstract description 11
- 230000035900 sweating Effects 0.000 claims description 7
- 230000011218 segmentation Effects 0.000 claims description 3
- 238000000926 separation method Methods 0.000 claims description 3
- 229910052751 metal Inorganic materials 0.000 claims description 2
- 239000002184 metal Substances 0.000 claims description 2
- 229910001220 stainless steel Inorganic materials 0.000 claims description 2
- 239000010935 stainless steel Substances 0.000 claims description 2
- 238000003466 welding Methods 0.000 claims description 2
- 239000007789 gas Substances 0.000 abstract description 50
- 238000013461 design Methods 0.000 abstract description 12
- 238000002156 mixing Methods 0.000 abstract description 9
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 9
- 230000015572 biosynthetic process Effects 0.000 abstract description 7
- 238000003786 synthesis reaction Methods 0.000 abstract description 7
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 abstract description 6
- 238000002485 combustion reaction Methods 0.000 abstract description 3
- 238000004519 manufacturing process Methods 0.000 abstract description 3
- 229910052757 nitrogen Inorganic materials 0.000 abstract description 3
- 230000003993 interaction Effects 0.000 abstract description 2
- 238000004064 recycling Methods 0.000 abstract 1
- 239000011269 tar Substances 0.000 description 16
- 210000004907 gland Anatomy 0.000 description 13
- 238000007789 sealing Methods 0.000 description 13
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 10
- 239000001301 oxygen Substances 0.000 description 10
- 229910052760 oxygen Inorganic materials 0.000 description 10
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical group O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 8
- 235000011089 carbon dioxide Nutrition 0.000 description 7
- 238000006243 chemical reaction Methods 0.000 description 7
- 238000000197 pyrolysis Methods 0.000 description 7
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 6
- 229910052799 carbon Inorganic materials 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 6
- 239000003546 flue gas Substances 0.000 description 6
- 239000011286 gas tar Substances 0.000 description 6
- 238000009413 insulation Methods 0.000 description 6
- 238000012546 transfer Methods 0.000 description 6
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 5
- 230000005540 biological transmission Effects 0.000 description 5
- 230000005587 bubbling Effects 0.000 description 5
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 4
- 238000011161 development Methods 0.000 description 4
- 230000018109 developmental process Effects 0.000 description 4
- 238000000034 method Methods 0.000 description 4
- 238000011084 recovery Methods 0.000 description 4
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 3
- 230000009286 beneficial effect Effects 0.000 description 3
- 239000003054 catalyst Substances 0.000 description 3
- 238000002955 isolation Methods 0.000 description 3
- JTJMJGYZQZDUJJ-UHFFFAOYSA-N phencyclidine Chemical class C1CCCCN1C1(C=2C=CC=CC=2)CCCCC1 JTJMJGYZQZDUJJ-UHFFFAOYSA-N 0.000 description 3
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 2
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 description 2
- 239000000292 calcium oxide Substances 0.000 description 2
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 2
- 230000009977 dual effect Effects 0.000 description 2
- 238000005243 fluidization Methods 0.000 description 2
- 230000017525 heat dissipation Effects 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 229910052742 iron Inorganic materials 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 238000004886 process control Methods 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- 230000009466 transformation Effects 0.000 description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- PWHULOQIROXLJO-UHFFFAOYSA-N Manganese Chemical compound [Mn] PWHULOQIROXLJO-UHFFFAOYSA-N 0.000 description 1
- 238000010504 bond cleavage reaction Methods 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 229910000019 calcium carbonate Inorganic materials 0.000 description 1
- JYYOBHFYCIDXHH-UHFFFAOYSA-N carbonic acid;hydrate Chemical compound O.OC(O)=O JYYOBHFYCIDXHH-UHFFFAOYSA-N 0.000 description 1
- 238000007233 catalytic pyrolysis Methods 0.000 description 1
- 239000011280 coal tar Substances 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 239000011285 coke tar Substances 0.000 description 1
- 239000000567 combustion gas Substances 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000010790 dilution Methods 0.000 description 1
- 239000012895 dilution Substances 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
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- 238000001125 extrusion Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- UQSXHKLRYXJYBZ-UHFFFAOYSA-N iron oxide Inorganic materials [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 description 1
- 229910052748 manganese Inorganic materials 0.000 description 1
- 239000011572 manganese Substances 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- NDLPOXTZKUMGOV-UHFFFAOYSA-N oxo(oxoferriooxy)iron hydrate Chemical compound O.O=[Fe]O[Fe]=O NDLPOXTZKUMGOV-UHFFFAOYSA-N 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 230000008092 positive effect Effects 0.000 description 1
- 238000006057 reforming reaction Methods 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 238000012827 research and development Methods 0.000 description 1
- 239000004576 sand Substances 0.000 description 1
- 230000007017 scission Effects 0.000 description 1
- 239000000377 silicon dioxide Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000000153 supplemental effect Effects 0.000 description 1
- 230000001502 supplementing effect Effects 0.000 description 1
- 239000005439 thermosphere Substances 0.000 description 1
- ABDKAPXRBAPSQN-UHFFFAOYSA-N veratrole Chemical compound COC1=CC=CC=C1OC ABDKAPXRBAPSQN-UHFFFAOYSA-N 0.000 description 1
Landscapes
- Fluidized-Bed Combustion And Resonant Combustion (AREA)
Abstract
The utility model relates to an indirect gasification system for biomass double fluidized beds. The double fluidized beds are in interaction to achieve combustion and indirect gasification to manufacture high-quality biomass synthesis gas, and the system comprises a fluidized bed combustor, a secondary cyclone separator of the fluidized bed combustor, a fluidized bed gasifier and secondary cyclone separator, a combustor air adding system, a combustor bed material feeding system, a gasifier water steam adding system, a gasifier biomass feeding system, a gasifier and combustor bed material circulating system, a bed material recycling device, a combustor and a gasifier pressure control system. The double-fluidized-bed indirect gasifier with inner circulation and outer circulation combined is adopted, nitrogen and the synthesis gas in air are naturally separated, the structural design of a reactor is improved, different bed materials are mixed to be used, a bed material circulating flowing system and the gas-solid mixing level are improved, gasification efficiency and the heat value of the synthesis gas are improved, the content of tar is reduced, and the high-quality synthesis gas is manufactured.
Description
Technical field
The utility model relates to a kind of biomass double fluidized-bed indirect gasification system of novel inner-outer circulation combination.
Background technology
The energy is the basis that modern society depends on for existence and development, and the situation is tense for the current energy resource supply of China, and environmental problem is serious, and development clean reproducible energy has become urgent problem.Biomass energy belongs to low-carbon (LC) clean energy, in the resource of state-owned abundant biological renewable energy, its research and development, popularize and contribute to reduce pollutant emission and improve the ecological environment.Biomass gasification technology is a kind of transform mode more clean and efficient compared with direct combustion, and synthetic gas both can be for heat production generating, synthol and chemical, also can hydrogen manufacturing.
No matter that fixed bed, moving-bed or fluidized-bed gasifier all can not well meet that tar content is few, flow rate is high, lower-cost requirement simultaneously at present.Lower (the <5MJ/Nm of the general calorific value of direct gasification technology synthetic gas
3), tar content is higher (sometimes up to >100g/Nm
3), updraft type fixed bed synthetic gas tar content is very large, calorific value is also lower; Although downdraft fixed bed gasifiers has reduced tar content, due to N
2dilution flow rate still lower, and technique is amplified difficulty, the higher (2-50g/Nm of tar content of general fluidized-bed gasifier synthetic gas
3), though two stage gasification can solve the problem of tar, flow rate is still lower.Thereby can effectively realizing the natural separation of nitrogen and synthetic gas in air, indirect gasification technology improves the calorific value of synthetic gas, very fast in North America and Europe development in recent years, but be also faced with that tar content is high, the problem of the each side such as optimization of the structure of reactor, bed material are selected, particles circulation flow system and process control, thereby the indirect gasification technology of being badly in need of development of new effectively reduces tar content, improves gasification efficiency and flow rate.
The patent US8241523B2(System and method for dual fluidized bed gasification of Rentech company of the U.S., in August, 2012) invent a set of double-fluidized-bed gasification system and prepared high-quality synthetic gas, but crude synthesis gas tar content is up to 10-150g/Nm
3, the reformer in gasifier downstream adopts nickel-base catalyst to reduce tar content, though there is the catalyzer of revivifier regeneration of deactivated, because nickel-base catalyst is more expensive, and human and environment is had to certain pollution, is difficult to process, and commercially produces so be difficult to realize.The patent US20130161563A1(Supplemental fuel to combustor of dual fluidized bed gasifier of another Rentech company, in June, 2013), thereby improve gasification efficiency with the combustion-supporting of inflammable gas to improve heat-transfer medium temperature, but synthetic gas tar content is still higher, crude synthesis gas tar content is up to 16g/Nm
3, and the use of inflammable gas has reduced the efficiency of whole system.The patent WO2007061301(Device for producing a product gas from biomass of the Dutch ECN in Europe, 2007) developed the double-fluidized-bed system of a kind of fast fluidized bed gasifier and bubbling style fluidized bed combustor, 850 DEG C of gasifier temperature, 930 DEG C of burner temperature, adopt rhombspar, peridotites and silica sand as main bed material, gas product is the synthetic gas that is rich in (>12v%) of methane, but because fast fluidized bed gasifier gas residence time is short, synthetic gas tar content is up to 20-30g/Nm
3.Chinese invention patent CN201990639U(two-part circulating fluidized bed biomass gasification system) a kind of two-part circulating fluidized bed biomass gasification system disclosed, biomass first gasify in fluidized-bed gasification furnace, utilize cyclonic separator that synthetic gas is separated with biomass char, biomass char is sent into cyclone combustion chamber and is carried out secondary pyrolysis, the combustion gas of secondary pyrolysis is sent vapourizing furnace back to supplementing energy, its principal feature is the abundant pyrolysis of the fixed carbon in biomass char, utilize its heat circulation to supply with vapourizing furnace simultaneously, shortcoming is after pyrolysis gas need to separate with tar, just to carry out secondary pyrolytic reaction afterwards, and the needed temperature of pyrolysis is high, although utilized fixed carbon heat in biomass char, but heat dissipation is large generally.Chinese invention patent CN102977927A has developed based on double-fluidized-bed gasifying biomass and has prepared device of synthetic gas and preparation method thereof, reformation fluidisation berth is above pyrolysis fluidized-bed, in reformation fluidized-bed, in calcium oxide and pyrolysis gas, the thermopositive reaction of carbonic acid gas forms calcium carbonate, promote water gas shift reaction and methanation reforming reaction, simultaneous oxidation calcium has katalysis to coke tar cracking, thereby has reduced tar content.The deficiency of this method is a material list one, mainly relies on calcium oxide, and its performing catalytic pyrolysis on tar is limited in one's ability, calcines in addition fluidized-bed temperature higher, reaches 950 DEG C, needs more coke, thereby has lowered vapourizing furnace gasification efficiency, and heat dissipation is also larger generally.
Although domestic and international double-fluidized-bed gasification technology has been obtained certain progress, the problem existing is also more.
Utility model content
The purpose of this utility model one is that the double-fluidized-bed indirect gasification system of a kind of inner-outer circulation combination of exploitation improves gasification efficiency to improve flow rate; Object two is further to reduce the coal-tar middle oil content of synthetic gas.
Realizing the utility model object technical scheme is: the double-fluidized-bed system that a kind of inner-outer circulation combines, interact and realize the gasification of burning and indirect heating, comprise successively fast fluidized bed burner, burner air adds system, burner bed material feed unit, two relatively parallel cyclonic separators of burner and a secondary cyclone, bubbling fluidized bed gasifier, gasifier water vapour adds system, gasifier biomass feed unit, material circulating system between gasifier and burner, the built-in cyclonic separator of gasifier, gasifier external cyclone water-separator, burner and gasifier pressure control system, can also comprise bed material recovery system, ash content shifts out system.
Within the part of fluidized bed combustor is placed in fluidized-bed gasifier, its top connects relative burner primary cyclone one and burner primary cyclone two; The tremie pipe one of burner primary cyclone one is to downward-extension, be deep in the bed of fluidized-bed gasifier bottom, burner primary cyclone one converges afterwards and is connected with burner secondary cyclone with the gas output tube of burner primary cyclone two; The inner upper end of fluidized-bed gasifier is provided with the built-in cyclonic separator of gasifier, it is connected with the tremie pipe two of burner primary cyclone two and the external cyclone water-separator being arranged on outside fluidized-bed gasifier respectively, the tremie pipe 3 16 of the built-in cyclonic separator 13 of gasifier is to downward-extension, be deep in the bed of fluidized-bed gasifier 2 bottoms, the built-in cyclonic separator of gasifier is connected by pipeline with gasifier external cyclone water-separator, preferably Venturi-type pipeline, the tremie pipe four of burner secondary cyclone connects and is connected with pipeline; The tremie pipe of gasifier external cyclone water-separator connects bed material retrieving arrangement, and bed material retrieving arrangement connects burner bed material feed unit; The tremie pipes six that comprise one or two in the bed of fluidized-bed gasifier bottom or more than three be connected tremie pipe five with horizontal screw bolt and be connected with burner bed material feed unit, gas output tube road Bonding pressure sensing and the control valve of burner secondary cyclone and gasifier external cyclone water-separator.
Above-mentioned biomass double fluidized-bed indirect gasification system, burner is fast fluidized bed reactor, is placed within gasifier to improve heat transfer efficiency, the raising gasifier gasification efficiency of burner to gasifier.Burner forms by two sections, the part of burner below sweating room be connected with burner above by flange be beneficial to handling.
Above-mentioned biomass double fluidized-bed indirect gasification system, bubbling style or turbulent fluidized bed gasifier are placed in outside burner, gasifier cross-sectional area is increased to meet the needs that gasification reaction volume increases gradually to top by bottom, reduce gas velocity simultaneously and carry secretly and extended the residence time of synthetic gas in gasifier to reduce material, reduce synthetic gas tar content.The different various piece of gasifier cross-sectional area is connected and is beneficial to handling by flange.
Above-mentioned biomass double fluidized-bed indirect gasification system, burner bottom has three air to add entrance, and at the nozzle place of burner bottommost two inlet mouths relative with burner bottom sides, air adds system to be connected by pipeline with burner respectively.
Above-mentioned biomass double fluidized-bed indirect gasification system, the water vapour of gasifier bottom adds two steam of having entered the room and adds entrance, and the burned device heat pipe wall of steam that enters sweating room further joins gasifier by the grid distributor of gasifier bottom after heating.
Above-mentioned biomass double fluidized-bed indirect gasification system, in the side of gasifier base unit, has two relative steam (or CO
2) entrance to be to improve gasifier gas-solid contact and fluidization level.Steam system is connected by pipeline with sweating room and gasifier bottom.
Above-mentioned biomass double fluidized-bed indirect gasification system, gasifier has a biomass feed unit, comprise biological screw handling machinery, carry and push the thermal material and the gas backmixing that design to realize continuous and stable charging and prevent gasifier by two mutual switches of ball valve, sealing gland and biological screw.Biological screw handling machinery is connected by flange with gasifier.
Above-mentioned biomass double fluidized-bed indirect gasification system, burner has a bed material feed system, comprise horizontal screw bolt feeder, push the thermal material and the gas backmixing that design to realize continuous and stable charging and prevent burner by two mutual switches of ball valve, sealing gland and screw rod transmission, water vapour or the carbonic acid gas sealing gland between horizontal screw bolt feeder and burner further prevents thermal material and hot gas back-mixing simultaneously.
Above-mentioned biomass double fluidized-bed indirect gasification system, gasifier has two bed material recycle systems, the material of gasifier is transported to respectively two horizontal screw bolt feeders below by two tremie pipes, designs to prevent gas leakage and the back-mixing between burner and gasifier by sealing gland and screw rod transmission extruding.Between tremie pipe and horizontal screw bolt feeder, connect by pipeline, horizontal screw bolt feeder is connected by pipeline or flange with burner.
Above-mentioned biomass double fluidized-bed indirect gasification system, the bed material of gasifier is mixture, is at least 2-3 kind of following material: oxygen carrier, nickel-base catalyst or the oxygen carrier of rhombohedral iron ore or the refuse that contains ferric oxide, Wingdale, rhombspar, ash content, iron-based, the oxygen carrier of manganese base, other catalyzer and oxygen carrier etc. natural or synthetic.
Above-mentioned biomass double fluidized-bed indirect gasification system, burner has two parallel primary cyclones, and the hott bed material of primary cyclone joins respectively the built-in cyclonic separator of gasifier bed and gasifier.
Above-mentioned biomass double fluidized-bed indirect gasification system, the primary cyclone two of burner is connected and has the securing gear of the twisting of preventing by pipeline with the cyclonic separator of gasifier inside, tremie pipe has certain inclination angle to ensure that material is at its low pressure position at the entrance that adds of cyclonic separator the inside, also can control the feeding rate of material in cyclonic separator the inside simultaneously in the part of the built-in cyclonic separator of gasifier the inside with vertical direction.
Above-mentioned biomass double fluidized-bed indirect gasification system, burner has a secondary cyclone, and the hott bed material of secondary cyclone joins the tubing system between two cyclonic separators of gasifier, preferably Venturi-type pipeline.Thermal material add the low pressure position of entrance in Venturi-type tubing system.
Above-mentioned biomass double fluidized-bed indirect gasification system, bed material reclaims and ash content collection realizes in reactor outside by the angle design of tremie pipe and the aperture of ball valve simultaneously.
Above-mentioned biomass double fluidized-bed indirect gasification system, the pressure equalization of burner and gasifier realizes by pressure sensing and control valve, and control valve can be arranged on the place of burner downstream flue-gas temperature 150-200 DEG C.
Above-mentioned biomass double fluidized-bed indirect gasification system, the bed material recovery system of burner secondary cyclone is transported to burner again by the feed system of burner, forms outer circulation, to improve material reaction transformation efficiency.
Above-mentioned biomass double fluidized-bed indirect gasification system, the Solid Bed material of separating is again transmitted back to gasifier bed by the built-in cyclonic separator of gasifier, forms internal recycle to improve gasification efficiency.
Above-mentioned biomass double fluidized-bed indirect gasification system, the biological carbon that the temperature of burner is not only formed by gasifier is controlled, also control to guarantee by oxygen carrier the heat that gasifier needs, oxygen carrier also provide oxygen to gasifier to improve gasification efficiency, to reduce tar content.
Above-mentioned biomass double fluidized-bed indirect gasification system, there is thermal insulation layer at the bottom of burner and top in the department of gasifier outside, and there is thermal insulation layer gasifier outside, and all cyclonic separator and hot channels that are placed in gasifier outside have thermal insulation layer.
Above-mentioned biomass double fluidized-bed indirect gasification system, the tremie pipe one of burner primary cyclone one, the tremie pipe three of the built-in cyclonic separator of gasifier go deep into fluidized-bed gasifier bottom, the exit, bottom of tremie pipe one and tremie pipe three and vertical direction are at an angle, the first half of exit end cross-sectional area seals by semicircle blind plate welding, the Lower Half of exit end cross-sectional area is the stainless steel metal thin slice that can open to inner rotary, to promote the material envelope of material to avoid the back-mixing of gas to flow backwards.
Above-mentioned fluidized bed combustor is placed in gasifier the inside, to improve the heat transfer efficiency of burner to gasifier.Gasifier operation temperature is at 750-800 DEG C, its biological carbon, oxygen carrier, catalyzer and other material are transported to burner continuously, and the cross-sectional area of gasifier increases to reduce gas velocity gradually to top by bottom, reduce material carries and extend residence time of synthetic gas secretly.In burner, the oxidizing reaction heat release of the burning of biological carbon and oxygen carrier raises the temperature of bed material and its gas, hott bed material is by the air conveying cyclonic separator that arrives, cyclonic separator and tremie pipe by burner join hott bed material inside the pipeline (preferably Venturi pipeline) of gasifier bed, gasifier cyclonic separator and gasifier outside, to improve the mixing of hott bed material and synthetic gas, thereby improve gasification efficiency and reduce tar content.The service temperature of burner can reach 850-900 DEG C, and its department in gasifier outside comprises that burner body, cyclonic separator and hot channel have thermal insulation layer, and gasifier outside also has thermal insulation layer to improve thermo-efficiency to reduce thermosteresis.Between burner and gasifier, isolate to prevent two gas leakage and back-mixings between reactor by water vapour or carbonic acid gas sealing gland and screw rod transmission extrusion system.Bed material reclaims and ash content collection is realized by angle and the ball valve of gasifier outside tremie pipe simultaneously.The recovery system that has surplus heat the flue gas of burner reclaims its heat, and the heat of gasifier synthetic gas can be used for producing steam or preheated air, carbonic acid gas and water vapour, makes system reach higher thermo-efficiency.
All there is unique distinction the utility model reactor and feed system structure design thereof, the preparation of bed material and mixing use, gas-solid mixing and particles circulation flow system and process control aspect thereof.
The utlity model has positive effect: the problem that (1) the utility model is low for biomass gasified synthesis gas calorific value, tar content is high, gasification efficiency is low, design the combine double-fluidized-bed interaction of novel inner-outer circulation and realized the system of burning and indirect gasification, burner is placed in gasifier the inside, improve greatly the heat transfer efficiency to gasifier by burner, burner and gasifier have thermal insulation separation thermosphere, have further reduced thermosteresis; (2) the hott bed material of burner is transported to respectively the preferred Venturi-type pipeline of gasifier bottom, gasifier cyclonic separator and gasifier pipeline the inside from its cyclonic separator, thus improved gasification temperature and gasification efficiency, the hott bed material that promoted to contain oxygen carrier and catalyzer with contain tar synthetic gas mix minimizing tar content; (3) between burner and gasifier, realize isolation by the design of steam or carbonic acid gas sealing gland and screw rod transmission extruding, thereby effectively realizing nitrogen and the effective of synthetic gas in air separates, greatly improved the calorific value of synthetic gas, thereby the flue gas of while burner can reclaim with residual neat recovering system the thermo-efficiency of its heat raising whole system; (4) the utility model gasifier biomass feed unit and burner bed material feed unit are realized conveying and the charging of stable and continuous and are prevented hot gas and the back-mixing of material by the design of two mutual switches of ball valve, carbonic acid gas sealing gland and screw rod transmission extruding, have also avoided the scission reaction in biomass feed system; (5) ash content is generally lighter, be easier to by air conveying to secondary cyclone, bed material reclaims and ash content collection is realized by the angle design of two tremie pipes of gasifier secondary cyclone and the control of ball valve simultaneously, avoid or reduced from gasifier and directly shifted out ash content, and the bed material of recovery is transported to burner and has further improved its transformation efficiency; (6) pressure that adopts pressure sensing and control valve to adjust burner and gasifier by burner flue gas (or intake air) flow makes it balanced, effectively guarantees the stable operation of material circulating system between two reactors.
Brief description of the drawings
For content of the present utility model is more easily expressly understood, according to specific embodiment also by reference to the accompanying drawings, the utility model is described in further detail, wherein below
Fig. 1 is that the utility model dissects structural representation;
Wherein: 1 fluidized bed combustor, 2 fluidized-bed gasifiers, 3 burner air add unit, 4 burner bed material feed unit, 5 gasifier biomass feed unit, 6 steam-pipes, 7 sweating rooms, 8 steam or CO
2inlet, 9 burner primary cyclone one, 10 burner primary cyclones two, 11 tremie pipe one, 12 burner secondary cyclones, the built-in cyclonic separator of 13 gasifier, 14 tremie pipe two, 15 gasifier external cyclone water-separators, 16 tremie pipes three, 17 pipelines, 18 four, 19 of tremie pipes material retrieving arrangements, 20 tremie pipes five, 21 tremie pipe six, 22 horizontal screw bolts, 23 pressure sensings and control valve.
Embodiment
(embodiment 1)
The present embodiment comprises that fluidized bed combustor 1 is for fast fluidized bed burner, fluidized-bed gasifier 2 is bubbling style fluidized-bed gasifier, it is three air intlets that burner air adds unit 3, the burner bed material feed unit 4 of fluidized bed combustor 1 bottom,, the sweating room 7 of the gasifier biomass feed unit 5 of fluidized-bed gasifier 2 middle and lower parts, the steam-pipe 6 of gasifier, gasifier bottom, the steam of gasifier bed side or CO
2inlet 8, being greater than within 2/3rds parts are placed in fluidized-bed gasifier 2 of fluidized bed combustor 1, its top is connected with relative burner primary cyclone 1 and burner primary cyclone 2 10, the tremie pipe 1 of burner primary cyclone 1 is to downward-extension, be deep in the bed of fluidized-bed gasifier 2 bottoms, burner primary cyclone 1 converges afterwards and is connected with burner secondary cyclone 12 with the output tube of burner primary cyclone 2 10, the inner upper end of fluidized-bed gasifier 2 is provided with the built-in cyclonic separator 13 of gasifier, it is connected with the tremie pipe 2 14 of burner primary cyclone 2 10 and the gasifier external cyclone water-separator 15 being arranged on outside fluidized-bed gasifier 2 respectively, the middle area of low pressure of built-in cyclonic separator 13 horizontal directions of gasifier that the isolated Solid Bed material of burner primary cyclone 2 10 is transported to fluidized-bed gasifier 2 by its tremie pipe 2 14, the built-in cyclonic separator 13 of gasifier is connected by the preferred Venturi-type pipeline 17 of pipeline with gasifier external cyclone water-separator 15, the tremie pipe 4 18 of burner secondary cyclone 12 connects and is connected with pipeline 17, the isolated Solid Bed material of the built-in cyclonic separator 13 of gasifier has tremie pipe 3 16 to return to gasifier bed, burner primary cyclone 2 10 is connected by pipeline with the built-in cyclonic separator 13 of gasifier and has a such as fastener of securing gear.The bottom of tremie pipe 1 and tremie pipe 3 16 is in vertical direction with 45o angle.The tremie pipe of gasifier external cyclone water-separator 15 connects bed material retrieving arrangement 19, and bed material retrieving arrangement 19 connects burner bed material feed unit 4; In fluidized-bed gasifier 2 bottom beds, there are 2 tremie pipes, respectively tremie pipe 5 20 and tremie pipe 6 21,1 tremie pipe 5 20 is connected with horizontal screw bolt 22, tremie pipe 6 21 is communicated with described burner bed material feed unit, realizes the circulation of bed material from fluidized-bed gasifier 2 to fluidized bed combustor 1; Gas output tube road Bonding pressure sensing and the control valve 23 of burner secondary cyclone 12 and gasifier external cyclone water-separator 15.Fluidized-bed gasifier 2 cross-sectional areas are increased to top segmentation gradually by bottom.The steam of bed side or CO
2inlet 8 is two relative inlet mouths.Fluidized bed combustor 1 bottom adopts flange to be connected so that load and unload with burner body part.
The present embodiment gasifier biomass feed unit 5 and bed material feed unit 4 are all used two mutual switches of ball valve, inside all adopts gas sealing gland, when charging, adopt horizontal screw bolt feeder to make biomass or the extruding of bed material closely and continuously feeding, described sealing gland gas comprises CO
2or N
2.In addition by the burner secondary cyclone 12 to fluidized bed combustor 1 and the piezometry in gasifier external cyclone water-separator 15 downstreams, the pressure that pressure sensing and control valve 23 are adjusted fluidized bed combustor 1 and fluidized-bed gasifier 2 by fluidized bed combustor 1 flue gas or its inlet air flow rate makes it balanced to guarantee the stable operation of material circulating system between two reactors, ensures that bed material is transported to cyclonic separator, pipeline 17 and the gasifier bed of gasifier by burner.In addition fluidized-bed gasifier 2 is regulated by the rotating speed of horizontal screw bolt to the mass transport speed of the bed material recycle system of fluidized bed combustor 1, and screw rod adopts carries extruding design to realize continuous and stable Matter Transfer and to prevent gas backmixing, and the water vapour that between tremie pipe 5 20, tremie pipe 6 21 and burner, connection portion adopts or carbonic acid gas sealing gland have further promoted effective isolation of fluidized-bed gasifier 2 and fluidized bed combustor 1.
(embodiment 2)
The present embodiment comprises that fluidized bed combustor 1 is for fast fluidized bed burner, fluidized-bed gasifier 2 is bubbling style fluidized-bed gasifier, it is three air intlets that burner air adds unit 3, the burner bed material feed unit 4 of fluidized bed combustor 1 bottom,, the sweating room 7 of the gasifier biomass feed unit 5 of fluidized-bed gasifier 2 middle and lower parts, the steam-pipe 6 of gasifier, gasifier bottom, the steam of gasifier bed side or CO
2inlet 8, being greater than within 2/3rds parts are placed in fluidized-bed gasifier 2 of fluidized bed combustor 1, its top is connected with relative burner primary cyclone 1 and burner primary cyclone 2 10, the tremie pipe 1 of burner primary cyclone 1 is to downward-extension, be deep in the bed of fluidized-bed gasifier 2 bottoms, burner primary cyclone 1 converges afterwards and is connected with burner secondary cyclone 12 with the output tube of burner primary cyclone 2 10, the inner upper end of fluidized-bed gasifier 2 is provided with the built-in cyclonic separator 13 of gasifier, it is connected with the tremie pipe 2 14 of burner primary cyclone 2 10 and the gasifier external cyclone water-separator 15 being arranged on outside fluidized-bed gasifier 2 respectively, the isolated Solid Bed material of burner primary cyclone 2 10 is transported to the middle area of low pressure of built-in cyclonic separator 13 horizontal directions of fluidized-bed gasifier 2 by its tremie pipe 2 14, the built-in cyclonic separator 13 of gasifier is connected by the preferred Venturi-type pipeline 17 of pipeline with gasifier external cyclone water-separator 15, the tremie pipe 4 18 of burner secondary cyclone 12 connects and is connected with pipeline 17, the isolated Solid Bed material of the built-in cyclonic separator 13 of gasifier has tremie pipe 3 16 to return to gasifier bed, burner primary cyclone 2 10 is connected by pipeline with the built-in cyclonic separator 13 of gasifier and has a such as fastener of securing gear.The bottom of tremie pipe 1 and tremie pipe 3 16 is in vertical direction with 35o angle.The tremie pipe of gasifier external cyclone water-separator 15 connects bed material retrieving arrangement 19, and bed material retrieving arrangement 19 connects burner bed material feed unit 4; 4 tremie pipes in fluidized-bed gasifier 2 bottom beds, respectively 5 20 and 1 tremie pipe 6 21 of 3 tremie pipes, tremie pipe 5 20 and tremie pipe 6 21 are vertical directions, the bore of tremie pipe hypomere is more bigger than epimere, tremie pipe 5 20 is connected with horizontal screw bolt 22, tremie pipe 6 21 is communicated with described burner bed material feed unit, realizes the circulation of bed material from fluidized-bed gasifier 2 to fluidized bed combustor 1; Gas output tube road Bonding pressure sensing and the control valve 23 of burner secondary cyclone 12 and gasifier external cyclone water-separator 15.Fluidized-bed gasifier 2 cross-sectional areas are increased to top segmentation gradually by bottom.The steam of bed side or CO
2inlet 8 is two relative inlet mouths.Fluidized bed combustor 1 bottom adopts flange to be connected so that load and unload with burner body part.
The present embodiment gasifier biomass feed unit 5 and bed material feed unit 4 are all used two mutual switches of ball valve, inside all adopts gas sealing gland, when charging, adopt horizontal screw bolt feeder to make biomass or the extruding of bed material closely and continuously feeding, described sealing gland gas comprises CO
2or N
2.In addition by the burner secondary cyclone 12 to fluidized bed combustor 1 and the piezometry in gasifier external cyclone water-separator 15 downstreams, the pressure that pressure sensing and control valve 23 are adjusted fluidized bed combustor 1 and fluidized-bed gasifier 2 by fluidized bed combustor 1 flue gas or its inlet air flow rate makes it balanced to guarantee the stable operation of material circulating system between two reactors, ensures that bed material is transported to cyclonic separator, pipeline 17 and the gasifier bed of gasifier by burner.In addition fluidized-bed gasifier 2 is regulated by the rotating speed of horizontal screw bolt to the mass transport speed of the bed material recycle system of fluidized bed combustor 1, and screw rod adopts carries extruding design to realize continuous and stable Matter Transfer and to prevent gas backmixing, and the water vapour that between tremie pipe 5 20, tremie pipe 6 21 and burner, connection portion adopts or carbonic acid gas sealing gland have further promoted effective isolation of fluidized-bed gasifier 2 and fluidized bed combustor 1.
Above-described specific embodiment; the purpose of this utility model, technical scheme and beneficial effect are further described; institute is understood that; the foregoing is only specific embodiment of the utility model; be not limited to the utility model; all within spirit of the present utility model and principle, any amendment of making, be equal to replacement, improvement etc., within all should being included in protection domain of the present utility model.
Claims (5)
1. a biomass double fluidized-bed indirect gasification system, comprise fluidized bed combustor (1), fluidized-bed gasifier (2), burner air adds unit (3), the burner bed material feed unit (4) of fluidized bed combustor (1) bottom, the sweating room (7) of the gasifier biomass feed unit (5) of fluidized-bed gasifier (2) middle and lower part, the steam-pipe (6) of gasifier, gasifier bottom, the steam of gasifier bed side or CO
2inlet (8), is characterized in that: within the part of fluidized bed combustor (1) is placed in fluidized-bed gasifier (2), its top is connected with relative burner primary cyclone one (9) and burner primary cyclone two (10), the tremie pipe one (11) of burner primary cyclone one (9) is to downward-extension, be deep in the bed of fluidized-bed gasifier (2) bottom, burner primary cyclone one (9) converges afterwards and is connected with burner secondary cyclone (12) with the output tube of burner primary cyclone two (10), the inner upper end of fluidized-bed gasifier (2) is provided with the built-in cyclonic separator of gasifier (13), it is connected with the tremie pipe two (14) of burner primary cyclone two (10) and the gasifier external cyclone water-separator (15) being arranged on outside fluidized-bed gasifier (2) respectively, the tremie pipe three (16) of the built-in cyclonic separator of gasifier (13) is to downward-extension, be deep in the bed of fluidized-bed gasifier (2) bottom, the built-in cyclonic separator of gasifier (13) is connected by pipeline (17) with gasifier external cyclone water-separator (15), the tremie pipe four (18) of burner secondary cyclone (12) connects and is connected with pipeline (17), the tremie pipe of gasifier external cyclone water-separator (15) connects bed material retrieving arrangement (19), and bed material retrieving arrangement (19) connects burner bed material feed unit (4), in the bed of fluidized-bed gasifier (2) bottom, there are at least 2 tremie pipes, comprise one or more tremie pipes five (20) that are connected with horizontal screw bolt (22) and the tremie pipe six (21) being connected with burner bed material feed unit (4), the gas output tube road Bonding pressure sensing of burner secondary cyclone (12) and gasifier external cyclone water-separator (15) and control valve (23).
2. biomass double fluidized-bed indirect gasification system according to claim 1, is characterized in that: fluidized-bed gasifier (2) cross-sectional area is increased to top segmentation gradually by bottom, the steam of bed side or CO
2inlet (8) is two relative inlet mouths.
3. according to biomass double fluidized-bed indirect gasification system described in claim 1 or 2, it is characterized in that: air adds from two relative inlet mouths of nozzle and its bottom sides of the lowermost end of burner (1) respectively, and the internal diameter of the part of burner (1) below gasifier bottom steam chamber (7) is more bigger than the internal diameter on burner (1) top.The steam of bed side or CO
2inlet (8) is two relative inlet mouths.
4. according to biomass double fluidized-bed indirect gasification system described in claim 1 or 2, it is characterized in that: the isolated Solid Bed material of described burner primary cyclone two (10) is transported to the middle area of low pressure of the built-in cyclonic separator horizontal direction of fluidized-bed gasifier (2) by its tremie pipe two (14), the built-in cyclonic separator of gasifier (13) is by the bed material of fluidized-bed gasifier (2) with from described burner primary cyclone two (10)
1isolated bed is expected gas solid separation again, isolated Solid Bed material turns back to fluidized-bed gasifier (2) bottom, gas is transported in the pipeline (17) of fluidized-bed gasifier (2) outside, and burner primary cyclone two (10) is connected by pipeline with the built-in cyclonic separator of gasifier (13) and has a securing gear.
5. biomass double fluidized-bed indirect gasification system according to claim 1, it is characterized in that: the tremie pipe one (11) of described burner primary cyclone one (9), the tremie pipe three (16) of the built-in cyclonic separator of gasifier (13) go deep into fluidized-bed gasifier (2) bottom, the exit, bottom of tremie pipe one (11) and tremie pipe three (16) and vertical direction are at an angle, the first half of exit end cross-sectional area seals by semicircle blind plate welding, and the Lower Half of exit end cross-sectional area is the stainless steel metal thin slice that can open to inner rotary.
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| CN201420183701.9U CN203794844U (en) | 2014-04-16 | 2014-04-16 | Indirect gasification system for biomass double fluidized beds |
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| CN201420183701.9U CN203794844U (en) | 2014-04-16 | 2014-04-16 | Indirect gasification system for biomass double fluidized beds |
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Cited By (9)
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| CN104862017A (en) * | 2015-05-07 | 2015-08-26 | 新奥科技发展有限公司 | Purification system and method for coal gas quality improvement |
| CN105018154A (en) * | 2014-04-16 | 2015-11-04 | 代建军 | Biomass double fluidized bed indirect gasification system and control method thereof |
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| CN105018154A (en) * | 2014-04-16 | 2015-11-04 | 代建军 | Biomass double fluidized bed indirect gasification system and control method thereof |
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| CN104862017A (en) * | 2015-05-07 | 2015-08-26 | 新奥科技发展有限公司 | Purification system and method for coal gas quality improvement |
| CN107787430A (en) * | 2015-06-15 | 2018-03-09 | 因姆普朗伯德公司 | Method for operating fluidized bed boiler |
| CN107743567A (en) * | 2015-06-15 | 2018-02-27 | 因姆普朗伯德公司 | Application of the ilmenite of pre-oxidation in fluidized-bed combustion boiler |
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| CN108753365B (en) * | 2018-05-28 | 2020-11-27 | 河南农业大学 | A device and process for preparing synthesis gas by reflux catalytic reforming |
| CN114729275A (en) * | 2019-11-25 | 2022-07-08 | 沃姆泽能源解决方案股份有限公司 | Coke making system and gasifier for all-steam gasification with carbon capture |
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