CN205295251U - Two sections pyrolysis gasification system of solid waste - Google Patents
Two sections pyrolysis gasification system of solid waste Download PDFInfo
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- CN205295251U CN205295251U CN201521071231.8U CN201521071231U CN205295251U CN 205295251 U CN205295251 U CN 205295251U CN 201521071231 U CN201521071231 U CN 201521071231U CN 205295251 U CN205295251 U CN 205295251U
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Abstract
The utility model relates to a two sections pyrolysis gasification system of solid waste has solid waste material charge -in system, pyrolysis apparatus, circulating fluidized bed oxidation vaporizer system, oxidation vaporizer cyclone and whirlwind disconnect -type reactor. The utility model discloses use circulating fluidized bed oxidation vaporizer that gas extracting pipe and sedimentation pipe combined together, remove pyrolytic reaction ware that bed and fluidized bed combined together and realize that two segmentation pyrolysis gasify to utilize whirlwind disconnect -type reactor to realize that thereby the intensive mixing of heat bed material and pyrolysis gas has greatly promoted tar schizolysis and gas purification, and the optimal design of by oxidation vaporizer and pyrolytic reaction ware structure, different bed material mix use, improvement that bed material circulation flow system and gas -solid mixing water were put down and charge -in system's improvement, can coproduction synthetic gas and pyrolysis gas, greatly improved whole pyrolysis gasification efficiency and pyrolysis gas calorific value, reduced synthetic gas and pyrolysis gas tar content, prepare out high -quality clean pyrolysis gas and synthetic gas.
Description
Technical field
This utility model relates to gasification of biomass furnace system, especially relates to a kind of two sections of pyrolysis gasification systems of solid waste.
Background technology
Utilizing in technology in biomass energy, biomass pyrogenation gasification technology is a kind of process that solid-state biomass is converted to gaseous fuel by thermal chemical reaction, and its gaseous product both may be used for generating, supply, it is also possible to for central heating. But traditional gasification technology also exists that fuel gases calorific value is low, tar content is high, waste water is difficult to the problems such as process, particularly fuel gases calorific value is low, the high subject matter that biomass gasification technology faces at present especially of tar content. Part biological pledge material low oxygen combustion is made owing to existing biomass gasification technology adopts, then heat that its flue gas has and the method that all the other biomass materials are carried out pyrolysis and gasification by remaining oxygen are utilized, a large amount of tar can be produced, no matter it is for generating electricity or supplying, all there is the problem that fuel gases calorific value is low and tar content is high. And tar meeting blocking pipeline, spark plug, pollution cylinder or fuel gas hole so that generating and supply all cannot be properly functioning, cause the cost of equipment cleaning and maintenance work to increase, the serious popularization and application hindering biomass pyrogenation gasification technology.
It is at present no matter fixing bed, moving bed or fluidized bed pyrolysis and gasifier all well can not meet that tar content is few, calorific value is high, lower-cost requirement simultaneously. Heating pyrolytic technique can effectively realize the natural separation of nitrogen and pyrolysis gas in air thus improve the calorific value of pyrolysis gas indirectly, at home and abroad development is very fast in recent years, but the problem being also faced with each side such as tar content height, optimization of the structure of reactor, bed selection, particles circulation flow system and process control, is badly in need of the pyrolysis gas solid waste conveyerisation technology of development of new thus effectively reducing tar and pollutant load, raising pyrolytic gasification efficiency and pyrolysis gas calorific value.
Utility model content
The purpose of this utility model is to solve problem set forth above, it is provided that a kind of two sections of pyrolysis gasification systems of solid waste prepared pyrolysis gas and synthesis gas simultaneously and improve pyrolysis gas calorific value and overall pyrolytic gasification efficiency and further minimizing pyrolysis gas and the coal-tar middle oil content with pollutant of synthesis gas.
The technical scheme realizing this utility model purpose is: two sections of pyrolysis gasification systems of this utility model one solid waste, having solid waste feed system, pyrolysis apparatus, recirculating fluidized bed oxidation gasifier system, oxidation gasifier cyclone separator and cyclone separating reactor, described solid waste feed system is connected with pyrolysis apparatus; The delivery outlet of described pyrolysis apparatus aoxidizes gasifier system by pipeline with recirculating fluidized bed and is connected; The outfan of described recirculating fluidized bed oxidation gasifier system is connected with the input of oxidation gasifier cyclone separator, the described outfan of oxidation gasifier cyclone separator is connected with the input of cyclone separating reactor, and described cyclone separating reactor is connected with pyrolysis apparatus.
Further prioritization scheme is described two sections of pyrolysis gasification systems of a kind of solid waste, described oxidation gasifier cyclone separator includes oxidation gasifier primary cyclone and oxidation gasifier secondary cyclone, described cyclone separating reactor includes one cyclonic separate type reactor and secondary rotary wind separate type reactor, the outfan of described oxidation gasifier primary cyclone connects one cyclonic separate type reactor, after the outfan of described oxidation gasifier secondary cyclone connects secondary rotary wind separate type reactor, it is connected with the input of material down-comer again.
Further prioritization scheme is described two sections of pyrolysis gasification systems of a kind of solid waste, described one cyclonic separate type reactor is arranged on the outside or inside of pyrolysis apparatus, when one cyclonic separate type reactor is arranged on pyrolysis apparatus outside, the outfan of one cyclonic separate type reactor is connected with pyrolysis apparatus. One cyclonic separate type reactor can improve heat transfer efficiency when being placed in inside pyrolysis apparatus.
Further prioritization scheme is described two sections of pyrolysis gasification systems of a kind of solid waste, described recirculating fluidized bed oxidation gasifier system includes sedimentation pipe, riser, slag discharge port successively, is positioned at the gas handling system bottom it and the steam generator being arranged on outside recirculating fluidized bed oxidation gasifier system tube wall, described riser and sedimentation pipe are asymmetric arrangement, and the delivery outlet of described sedimentation pipe is connected with the input port of pyrolysis apparatus by tremie pipe.
Further prioritization scheme is described two sections of pyrolysis gasification systems of a kind of solid waste, described recirculating fluidized bed oxidation gasifier system includes sedimentation pipe, riser, slag discharge port successively, is positioned at the gas handling system bottom it and the steam generator being arranged on outside cyclic oxidation gasifier system tube wall, described riser is different with sedimentation pipe diameter, and it is set to asymmetric arrangement, namely riser deflection is arranged on the side of sedimentation pipe, and the delivery outlet of described sedimentation pipe is connected with the input port of pyrolysis apparatus by tremie pipe. Recirculating fluidized bed oxidation gasifier system adopts the fluidized-bed structure form that riser and sedimentation pipe combine, riser and sedimentation pipe adopt asymmetric arrangement so that the bigger bed particle packing side below sedimentation pipe, be conducive to realizing effectively expecting envelope to bulky grain discharge nozzle and tremie pipe, these bulky grains are directly transported to pyrolysis apparatus, it is to avoid cyclone separator and in abrasion.
Further prioritization scheme is described two sections of pyrolysis gasification systems of a kind of solid waste, described recirculating fluidized bed oxidation gasifier system adopts the single tube reactor of same diameter, and it includes riser, slag discharge port successively, is positioned at the gas handling system bottom it and the steam generator being arranged on outside recirculating fluidized bed oxidation gasifier system tube wall.
Further prioritization scheme is described two sections of pyrolysis gasification systems of a kind of solid waste, the screw feeder that material feed end is level of described pyrolysis apparatus, the main body of described pyrolysis apparatus is that base plate has acclive fluidized-bed reactor, having hole on described base plate, the mode of heating of described pyrolysis apparatus can be microwave heating or electrical heating.
Further prioritization scheme is described two sections of pyrolysis gasification systems of a kind of solid waste, and the input of described material down-comer connects solid waste conveyer, and solid waste is transported in material down-comer by conveyer, and eventually enters in pyrolysis apparatus. Material in material down-comer has material envelope effect.
Further prioritization scheme is described two sections of pyrolysis gasification systems of a kind of solid waste, and the described outfan of oxidation gasifier cyclone separator is connected with the input of heat production electricity generation system. The outfan of described cyclone separating reactor is connected with the input of gas cooling and cleaning system.
This utility model is a kind of two sections of pyrolysis gasification systems of solid waste based on fluid bed and moving bed, and fluid bed and moving bed interact and realize burning, partial oxidation and gasification and prepare synthesis gas and prepare high quality heat by pyrolysis reactor and vent one's spleen. This utility model uses the pyrolysis apparatus that recirculating fluidized bed oxidation gasifier, moving bed and fluid bed combine to realize two-part pyrolytic gasification, utilizes cyclone separating reactor to realize being sufficiently mixed with abundant cracking reformation tar, elimination pollutant of hott bed material and pyrolysis gas.
After two cyclone separator of recirculating fluidized bed oxidation gasifier system downstream realize gas solid separation, hott bed material respectively enters two cyclone separating reactors of pyrolysis apparatus, then hott bed material is respectively enterd inside pyrolysis apparatus by two cyclone separating reactors and the down-comer of feed system, and solid waste and bed mixture are transported to pyrolysis apparatus by screw feeder. The bed of larger particles can be delivered directly to pyrolysis apparatus by the tremie pipe of the sedimentation pipe lower end of recirculating fluidized bed oxidation gasifier. Go to downstream from cyclone separator synthesis gas out, or the gas handling system returning to recirculating fluidized bed oxidation gasifier system is used as fuel; Downstream can be gone to from cyclone separating reactor pyrolysis gas out or return to the gas handling system of recirculating fluidized bed oxidation gasifier system and be used as fuel. The gas handling system of recirculating fluidized bed oxidation gasifier system bottom passes into air and the synthesis gas of circulation, pyrolysis gas or dusty fuel (such as charcoal or powdery biomass granule), mixed combustion produces high-temperature area and makes ash fusion, fall after slag cooling and discharged by bottom oxidation gasifier, having burning, partial oxidation and gasification reaction to occur inside oxidation gasifier, its gaseous product is synthesis gas; The material feed end of pyrolysis apparatus is the screw feeder of level, and pyrolysis apparatus main body can be the acclive fluid bed of base plate and the reactor of moving bed combination, and porose on base plate, fluidizing agent is steam or other gas.
This utility model adopts pressure sensing and controls valve, adjust the pressure of oxidation gasifier and pyrolysis apparatus so as to equilibrium by downstream burners flue gas or oxidation gasification reaction device inlet air flow rate and air-fuel ratio, effectively guarantee the stable operation of material circulating system between two reactors.
This utility model has positive effect: pyrolysis gas and synthesis gas can be simultaneously generated by (1) system of the present utility model in two reactors of same device, not only increase pyrolytic gasification efficiency, and decrease tar and pollutant emission. Synthesis gas and pyrolysis gas are without pollutant such as dioxin, and the synergism of thermophore, catalyst and charcoal etc. is farthest to reduce tar and pollutant emission content.
(2) pyrolysis apparatus adopts the structural design that fluid bed and moving bed combine, adopt the particle flow pattern that screw rod transmission, gravity transfer and fluidisation combine, add the motility of pyrolysis system stability and operation, improve the adaptability to ash fusion bonding.
(3) join pyrolysis apparatus at Liang Chu respectively from the hott bed material of recirculating fluidized bed oxidation gasifier system and form two-period form pyrolysis apparatus, hott bed material is not only sufficiently mixed with raw material, and the pyrolysis gas in cyclone separating reactor with containing tar is sufficiently mixed thus farthest decreasing pyrolysis gas tar content, it is beneficial to pyrolysis apparatus system desulfurization dechlorination, improves pyrolytic gasification efficiency.
Wherein recirculating fluidized bed oxidation gasifier system can adopt the single tube reactor that diameter is consistent, may be used without riser and fluidized-bed structure form that sedimentation pipe combines, fluid bed riser and sedimentation pipe adopt asymmetric arrangement so that the bigger bed particle packing side below sedimentation pipe, be conducive to realizing effectively expecting envelope to bulky grain discharge nozzle and tremie pipe, these bulky grains are directly transported to pyrolysis apparatus, it is to avoid abrasion in cyclone separator.
(4) cyclone separating reactor is used for the mixing of strengthening hott bed material and pyrolysis gas further, reduces pyrolysis gas tar content. Pyrolysis apparatus cyclone separating reactor is placed in inside pyrolysis apparatus to improve heat transfer efficiency.
(5) gas handling system of recirculating fluidized bed oxidation gasifier system bottom passes into air and the synthesis gas of circulation, pyrolysis gas or dusty fuel (such as the charcoal reclaimed or powdered biomass), mixed combustion radial direction zone line bottom oxidation gasifier produces high temperature makes ash fusion, falling after slag cooling and discharged by bottom oxidation gasifier, slag has recycle value. Steam generator can be provided with outside the burning zone of oxidation gasification reaction device to utilize its heat to produce steam, be beneficial to cooling and the discharge of slag simultaneously. Having burning, partial oxidation and gasification reaction to occur inside oxidation gasification reaction device, its gaseous product is synthesis gas.
Accompanying drawing explanation
In order to make content of the present utility model be easier to be clearly understood, below according to specific embodiment and in conjunction with accompanying drawing, this utility model is described in further detail, wherein
Fig. 1 is structural representation of the present utility model;
Fig. 2 is the structural representation of embodiment 2;
Accompanying drawing labelling: 1, solid waste feed system, 2, pyrolysis apparatus, 3, one cyclonic separate type reactor, 4, tremie pipe, 5, recirculating fluidized bed oxidation gasifier system, 6, gas handling system, 7, riser, 8, sedimentation pipe, 9, steam generator, 10, oxidation gasifier primary cyclone, 11, oxidation gasifier secondary cyclone, 12, secondary rotary wind separate type reactor, 13, screw feeder, 14, material down-comer, 15, solid waste conveyer, 16, solid waste, 17, synthesis gas, 18, heat production electricity generation system, 19, pyrolysis gas, 20, gas cooling and cleaning system, 21 slag discharge ports.
Detailed description of the invention
(embodiment 1)
As shown in Figure 1, two sections of pyrolysis gasification systems of the solid waste that this utility model has, having solid waste feed system 1, pyrolysis apparatus 2, recirculating fluidized bed oxidation gasifier system 5, oxidation gasifier cyclone separator and cyclone separating reactor, wherein solid waste feed system 1 is connected with pyrolysis apparatus 2; The delivery outlet of pyrolysis apparatus 2 aoxidizes gasifier system 5 by pipeline with recirculating fluidized bed and is connected; The outfan of recirculating fluidized bed oxidation gasifier system 5 is connected with the input of oxidation gasifier cyclone separator, and the outfan of oxidation gasifier cyclone separator is connected with cyclone separating reactor, and cyclone separating reactor is connected with pyrolysis apparatus 2.
Wherein oxidation gasifier cyclone separator includes oxidation gasifier primary cyclone 10 and oxidation gasifier secondary cyclone 11. Cyclone separating reactor includes one cyclonic separate type reactor 3 and secondary rotary wind separate type reactor 12, the outfan of oxidation gasifier primary cyclone 10 connects one cyclonic separate type reactor 3, after the outfan of oxidation gasifier secondary cyclone 11 connects secondary rotary wind separate type reactor 12, then it is connected with the input of material down-comer 14.
One cyclonic separate type reactor 3 is arranged on the outside or inside of pyrolysis apparatus 2. Described recirculating fluidized bed oxidation gasifier system 5 includes sedimentation pipe 8, riser 7 successively, is positioned at the gas handling system 6 bottom it and the steam generator 9 being arranged on outside recirculating fluidized bed oxidation gasifier system 5 tube wall, and slag discharge port 21, two pipe fittings that riser 7 and sedimentation pipe 8 differ for diameter, sedimentation pipe 8 is set on riser 7, and asymmetric arrangement, namely riser 7 is partial to sedimentation pipe 8 side, the bottom of sedimentation pipe 8 has delivery outlet, bigger bed granule passes through tremie pipe 4, through the input port of pyrolysis apparatus 2, enter in pyrolysis apparatus 2.
The wherein screw feeder that material feed end is level 13 of pyrolysis apparatus 2, screw feeder 13 is deep in the middle part of pyrolysis apparatus 2 in the cavity of pyrolysis section, the body cavity of described pyrolysis apparatus 2 is that base plate has acclive fluid bed and the reactor of moving bed combination, having hole on described base plate, the mode of heating of described pyrolysis apparatus 2 can be microwave heating or electrical heating. The input of the material down-comer 14 of solid waste feed system 1 connects solid waste conveyer 15, and solid waste 16 is transported in material down-comer 14 by solid waste conveyer 15. Supplementary bed can add at solid waste conveyer 15 place. The outfan of oxidation gasifier cyclone separator is connected with the input of heat production electricity generation system 18, and the synthesis gas 17 produced in oxidation gasifier cyclone separator can be transferred in heat production electricity generation system 18. Outfan in cyclone separating reactor is connected with the input of gas cooling and cleaning system 20, and the pyrolysis gas 19 that cyclone separating reactor produces can be transferred in gas cooling and cleaning system 20.
Its work process is: the gas handling system 6 at recirculating fluidized bed oxidation gasifier system 5 passes into air and the synthesis gas come or pyrolysis gas (or powdery solid fuel) are circulated thus there is oxidation and partial oxidation reaction (burning completely and partial combustion) in downstream, burning produce high temperature make ash melt formed slag discharged by bottom, recirculating fluidized bed oxidation gasifier system 5 be provided externally with steam generator 9; The gas that oxidation produces is mainly the CO of high temperature2��H2O and CO (CO is imperfect combustion product), the charcoal generating gasification reaction in these gases and bed generates CO and H2, the gas product of generation is mainly CO2��H2O��CO��H2And CH4, be called synthesis gas here. This synthesis gas can be used for producing steam, and some vapor returns pyrolysis apparatus 2 and recirculating fluidized bed oxidation gasifier system 5 as fluidizing agent.
Recirculating fluidized bed oxidation gasifier system 5 adopts the fluidized-bed structure form that riser 7 and sedimentation pipe 8 combine, riser 7 and sedimentation pipe 8 adopt asymmetric arrangement so that the bigger bed particle packing side below sedimentation pipe 8, be conducive to realizing bulky grain discharge nozzle and tremie pipe 4 effectively expecting envelope, these bulky grains are directly transported in pyrolysis apparatus 2, it is to avoid the abrasion in oxidation gasifier primary cyclone 10 and oxidation gasifier secondary cyclone 11.The hott bed material of recirculating fluidized bed oxidation gasifier system 5 enters in one cyclonic separate type reactor 3 and secondary rotary wind separate type reactor 12 after the gas solid separation of oxidation gasifier primary cyclone 10 and oxidation gasifier secondary cyclone 11, hott bed material and the pyrolysis gas containing tar are sufficiently mixed thus farthest decreasing pyrolysis gas tar content, it is beneficial to pyrolysis apparatus system desulfurization dechlorination, also improves system pyrolytic gasification efficiency. The hott bed material separated from one cyclonic separate type reactor 3 and secondary rotary wind separate type reactor 12 respectively enters the material down-comer 14 of pyrolysis apparatus 2 and feed system and forms two-period form pyrolysis apparatus (containing dryer section and pyrolysis section), one cyclonic separate type reactor 3 is placed in improve heat transfer efficiency inside pyrolysis apparatus 2, and the isolated solid bed of one cyclonic separate type reactor 3 enters inside pyrolysis apparatus 2 through a bend pipe; Pyrolysis gas 19 after gas solid separation enters gas cooling and the cleaning system 20 in downstream. Solid waste is entered pyrolysis apparatus 2 by solid waste feed system, feed system adopts the sealing means that screw rod transmission extruding and Starlike valve combine, screw feeder 13 is deep into inside pyrolysis apparatus 2, deep screw rod can stir further and distribute bed material, being pyrolyzed device 2 internal high temperature to heat, screw rod and the hott bed material from recirculating fluidized bed oxidation gasifier system 5 transfer heat to solid waste and play its preheating and dry effect simultaneously; Enter screw portion within the pyrolysis apparatus 2 hott bed material also with from tremie pipe 4 to contact with each other and friction, it is to avoid the bonding of tar and carbon distribution on screw rod. Solid waste and the hott bed material added with one cyclonic separate type reactor 3 from tremie pipe 4 after preheating and dried mix generation pyrolytic reaction.
Pyrolysis apparatus 2 adopts the structural design that fluid bed and moving bed combine, adopt the particle flow pattern that screw rod transmission, gravity transfer (base plate has slope) and fluidisation (base plate is porose) combine, add the motility of pyrolysis system stability and operation, improve the adaptability to ash fusion bonding. By the improvement of the improvement of pyrolysis reactor structural design and bed blood circulation, charcoal in bed and catalyst can by major part coke tar cracking, thus pyrolysis gas coal-tar middle oil content is greatly lowered. Charcoal and other bed overflow that pyrolysis apparatus 2 produces aoxidize gasifier system 5 to recirculating fluidized bed. Wherein pyrolysis apparatus 2 microwave heating or electrically heated mode improves pyrolysis temperature, thus improving pyrolysis product distribution and composition, adopts microwave heating, and pyrolysis apparatus need to use pottery or quartz tube reactor and with charcoal and bed for microwave absorption.
Except charcoal, bed mainly includes thermophore and catalyst etc., and these bed synergism are farthest to reduce tar content and pollutant emission. By the optimization design of the improvement of pyrolysis and oxidation gasification reaction device feed system, oxidation gasifier and pyrolysis apparatus structural shape, different bed mixing uses, bed circulates system and the raising of gas-solid mixed-level, native system can produce synthesis gas and pyrolysis gas simultaneously, drastically increase overall pyrolytic gasification efficiency, improve pyrolysis gas calorific value, decrease synthesis gas and pyrolysis gas tar content, synthesis gas and pyrolysis gas are without pollutant such as dioxin, thus effectively preparing cleaning pyrolysis gas and the synthesis gas of high-quality.
(embodiment 2)
As shown in Figure 2, the single tube reactor of same diameter is adopted, its steam generator 9 including riser 7 successively, being positioned at the gas handling system 6 bottom it, slag discharge port 21 and be arranged on outside recirculating fluidized bed oxidation gasifier system 5 tube wall with the described recirculating fluidized bed oxidation gasifier system 5 that is distinguished by implementing 1.
Particular embodiments described above; the purpose of this utility model, technical scheme and beneficial effect have been further described; it is it should be understood that; the foregoing is only specific embodiment of the utility model; it is not limited to this utility model; all within spirit of the present utility model and principle, any amendment of making, equivalent replacement, improvement etc., should be included within protection domain of the present utility model.
Claims (9)
1. two sections of pyrolysis gasification systems of a solid waste, it is characterized in that: having solid waste feed system (1), pyrolysis apparatus (2), recirculating fluidized bed oxidation gasifier system (5), oxidation gasifier cyclone separator and cyclone separating reactor, described solid waste feed system (1) is connected with pyrolysis apparatus (2); The delivery outlet of described pyrolysis apparatus (2) aoxidizes gasifier system (5) by pipeline with recirculating fluidized bed and is connected; The outfan of described recirculating fluidized bed oxidation gasifier system (5) is connected with the input of oxidation gasifier cyclone separator, the described outfan of oxidation gasifier cyclone separator is connected with the input of cyclone separating reactor, and described cyclone separating reactor is connected with pyrolysis apparatus (2).
2. a kind of two sections of pyrolysis gasification systems of solid waste according to claim 1, it is characterized in that: described oxidation gasifier cyclone separator includes oxidation gasifier primary cyclone (10) and oxidation gasifier secondary cyclone (11), described cyclone separating reactor includes one cyclonic separate type reactor (3) and secondary rotary wind separate type reactor (12), the outfan of described oxidation gasifier primary cyclone (10) connects one cyclonic separate type reactor (3), after the outfan of described oxidation gasifier secondary cyclone (11) connects secondary rotary wind separate type reactor (12), it is connected with the input of material down-comer (14) again, the outfan of described oxidation gasifier secondary cyclone (11) also can be directly connected to pyrolysis apparatus (2).
3. a kind of two sections of pyrolysis gasification systems of solid waste according to claim 2, it is characterized in that: described one cyclonic separate type reactor (3) is arranged on the outside or inside of pyrolysis apparatus (2), when one cyclonic separate type reactor (3) is arranged on pyrolysis apparatus (2) outside, the outfan of one cyclonic separate type reactor (3) is connected with pyrolysis apparatus (2).
4. a kind of two sections of pyrolysis gasification systems of solid waste according to claim 1, it is characterized in that: described recirculating fluidized bed oxidation gasifier system (5) includes sedimentation pipe (8) successively, riser (7), slag discharge port (21), it is positioned at the gas handling system bottom it (6) and the steam generator (9) being arranged on outside recirculating fluidized bed oxidation gasifier system (5) tube wall, described riser (7) is different with sedimentation pipe (8) diameter, and it is set to asymmetric arrangement, riser (7) deflection is arranged on the side of sedimentation pipe (8), the delivery outlet of described sedimentation pipe (8) is connected with the input port of pyrolysis apparatus (2) by tremie pipe (4).
5. a kind of two sections of pyrolysis gasification systems of solid waste according to claim 1, it is characterized in that: described recirculating fluidized bed oxidation gasifier system (5) adopts the single tube reactor of same diameter, it includes riser (7), slag discharge port (21) successively, is positioned at the gas handling system (6) bottom it and the steam generator (9) being arranged on outside recirculating fluidized bed oxidation gasifier system (5) tube wall.
6. a kind of two sections of pyrolysis gasification systems of solid waste according to claim 1, it is characterized in that: the screw feeder that material feed end is level (13) of described pyrolysis apparatus (2), the main body of described pyrolysis apparatus (2) is that base plate has acclive fluid bed and the reactor of moving bed combination, having hole on described base plate, the mode of heating of described pyrolysis apparatus (2) can be microwave heating or electrical heating.
7. a kind of two sections of pyrolysis gasification systems of solid waste according to claim 1, it is characterized in that: the input of described material down-comer (14) connects solid waste conveyer (15) and secondary rotary wind separate type reactor (12), solid waste (16) is transported in material down-comer (14) by solid waste conveyer (15), and eventually enter in pyrolysis apparatus (2), reactor supplements bed and can be added by solid waste conveyer (15), the outfan of secondary rotary wind separate type reactor (12) and material down-comer (14) connect, also can directly connect with the centre of screw feeder (13) and distal portion.
8. a kind of two sections of pyrolysis gasification systems of solid waste according to claim 1, it is characterized in that: the outfan of described oxidation gasifier cyclone separator (11) is connected with the input of heat production electricity generation system (18), the outfan of cyclone separating reactor (12) is connected with the input of gas cooling and cleaning system (20).
9. a kind of two sections of pyrolysis gasification systems of solid waste according to claim 1, it is characterized in that: described recirculating fluidized bed oxidation gasifier system (5) bottom passes into air and combustion gas or powdery solid fuel, occur burning and partial oxidation reaction to produce high temperature; The position that high-temperature gas aoxidizes gasifier system (5) bottom radially middle at recirculating fluidized bed enters, slag is discharged by slag discharge port (21) below, and air and fuel are added system and connected by pipeline and recirculating fluidized bed oxidation gasifier system (5).
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| Application Number | Priority Date | Filing Date | Title |
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| CN201521071231.8U CN205295251U (en) | 2015-12-21 | 2015-12-21 | Two sections pyrolysis gasification system of solid waste |
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| CN201521071231.8U CN205295251U (en) | 2015-12-21 | 2015-12-21 | Two sections pyrolysis gasification system of solid waste |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105419878A (en) * | 2015-12-21 | 2016-03-23 | 代建军 | Two-section pyrolysis and gasification system of solid waste |
| CN108889300A (en) * | 2018-06-04 | 2018-11-27 | 中国科学院生态环境研究中心 | A kind of preparation method and applications of novel hydro-thermal charcoal carried nanometer bi-metal catalyst |
| CN109181781A (en) * | 2018-11-01 | 2019-01-11 | 大连海洋大学 | The method and its used equipment of synthesis gas are prepared using the biomass comprising seaweed |
-
2015
- 2015-12-21 CN CN201521071231.8U patent/CN205295251U/en not_active Withdrawn - After Issue
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105419878A (en) * | 2015-12-21 | 2016-03-23 | 代建军 | Two-section pyrolysis and gasification system of solid waste |
| CN105419878B (en) * | 2015-12-21 | 2018-07-03 | 代建军 | A kind of two sections of pyrolysis gasification systems of solid waste |
| CN108889300A (en) * | 2018-06-04 | 2018-11-27 | 中国科学院生态环境研究中心 | A kind of preparation method and applications of novel hydro-thermal charcoal carried nanometer bi-metal catalyst |
| CN109181781A (en) * | 2018-11-01 | 2019-01-11 | 大连海洋大学 | The method and its used equipment of synthesis gas are prepared using the biomass comprising seaweed |
| CN109181781B (en) * | 2018-11-01 | 2020-08-18 | 大连海洋大学 | Method for preparing synthesis gas by utilizing biomass containing seaweed and equipment adopted by method |
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