CN105368472A - Pyrolysis apparatus and method - Google Patents
Pyrolysis apparatus and method Download PDFInfo
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- CN105368472A CN105368472A CN201510890848.0A CN201510890848A CN105368472A CN 105368472 A CN105368472 A CN 105368472A CN 201510890848 A CN201510890848 A CN 201510890848A CN 105368472 A CN105368472 A CN 105368472A
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- pyrolysis
- gas
- catalyzer
- catalyst
- semicoke
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
- C10B53/04—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of powdered coal
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B47/00—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion
- C10B47/18—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with moving charge
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
- C10B53/08—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form in the form of briquettes, lumps and the like
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
- C10B57/08—Non-mechanical pretreatment of the charge, e.g. desulfurization
- C10B57/10—Drying
Abstract
The invention provides a pyrolysis apparatus and method. The apparatus includes the following parts: a pyrolysis material hopper; a first feeding device, which is connected with the pyrolysis material hopper; a pyrolysis reactor, which comprises an oil-gas mixture outlet, a pyrolysis material inlet and a semi-coke outlet, wherein the pyrolysis material inlet is connected with the first feeding device; a catalyst adding device; a condensation recovery device, which is connected with the oil-gas mixture outlet; and a semi-coke conveyor, which is connected with the semi-coke outlet. The device adds catalyst to the pyrolysis reactor through a catalyst spray pipeline, so that the catalyst is uniformly mixed with the pyrolysis material in the pyrolysis reactor to improve the catalytic efficiency.
Description
Technical field
The present invention relates to pyrolytic technique field, particularly, relate to pyrolysis plant and method.
Background technology
Sweet natural gas, due to its clean environment firendly performance, is a kind of very valuable resource, and the energy structure feature of China is " many coals, oil starvation, weak breath ", and therefore coal liquifaction and gas maked coal are the outlets solving energy problem of China.Gas maked coal technical process is complicated, scale of investment is comparatively large, and water resources consumption is large, becomes the bottleneck of restriction gas maked coal development.Coal low-temperature pyrolysis, product can fully utilize (oil, gas, semicoke), can improve added value, increases economic benefit, can reduce again the environmental pollution that fire coal causes, be considered to the effective approach of coal high-efficiency clean utilization.Existing hot solid carrier devolatilization technique and the multistage rotary kiln pyrolytic process mainly containing three river side's stoves, the greatly work of China for industrial coal pyrolysis technique, external Wood stove, the strange three sections of stoves in Shandong, Kao Baisi stove and LFC retorting technique etc.The Particle size requirements of some destructive distillation type of furnaces to raw material is high, can only pyrolysis lumped coal, causes small particles material to make full use of, the not high and problem of bulk deposition contaminate environment of resource utilization; The oily yield of some type of furnaces is lower, and is heating carrier with gas, and cause condensate recovery system huge, pyrogenation and carbonization gas is rushed rare, and gas heating value is low, is difficult to the problems such as comprehensive utilization further; The pyrolysis type of furnace of some solid thermal carriers, then there is raw material and mix with thermal barrier, and thermal barrier reheats the operations such as back-mixing, and technique is comparatively complicated, equipment is more, manufacturing cost and working cost high.In addition, all to produce for the purpose of a large amount of tar in existing industrial pyrolytic process, pyrolysis gas output is less, or pyrolysis gas by following cycle technique utilization of burning, What is more to the pyrolytic gas making of coal and liquefaction degree all inadequate.
Thus, current pyrolytic process of coal still haves much room for improvement.
Summary of the invention
The present invention is intended to solve one of technical problem in correlation technique at least to a certain extent.For this reason, one object of the present invention be to propose a kind of low to coal Particle size requirements, fast pyrogenation and catalytic pyrolysis technology are merged mutually, pyrolysis oil yield pyrolytic process that is high or that heat without the need to gas, solid thermal barrier.
The present invention completes based on the following discovery of contriver:
The technological process of one of the dry distillation of coal device conventional at present strange three sections of stoves in German Shandong is as follows: first the qualified shove charge coal (particle diameter 20-80mm) shipped by standby coal workshop section loads in the coal bunker of furnace roof topmost, the dryer section of gas retort is loaded again through opening for feed and auxiliary coal bin, dried and be preheating to 150 DEG C with the reverse contact heat-exchanging of cycling hot air-flow.Dried coal enters retort section through some uprises, with hot gas flow reverse contact be heated to 500 ~ 850 DEG C at carry out middle low-temperature pyrolysis and generate semicoke and dry distillation gas.At hypomere, the semicoke circulating current that is cooled is cooled to 100 ~ 150 DEG C of discharges, and circulation gas and dry distillation gas mixture are drawn by the raw coke oven gas pipe of retort section, wherein liquid product extraction in subsequent condensation cooling separation.Most purification coal gas delivers to dryer section and retort section roasting kiln, and some directly sends into semicoke cooling section, and residual gas is sent outside.But, Germany's Shandong strange three sections of stoves to the granularity (20 ~ 80mm) of feed coal and coal quality requirements high, raw material availability is low, gaseous heat-carrier heat supply, reduces the calorific value of carbonization gas, cause condensate recovery system and equipment huge, adopt wet quenching, the feature of environmental protection is poor, and semicoke must be again dry, and it is abundant not to carry oil to the pyrolysis of feed coal.Another kind of conventional LFC distillation process utilizes heat smoke to carry out drying to oil shale particle raw material, the high-temperature flue gas adopting semicoke or carbonization gas burning to produce carries out indirect heating to dry oil shale particle and realizes pyrolysis, obtain high-temperature oil gas and semicoke, high-temperature oil gas is filtered and after heat exchange, carries out fractionation and obtain gasoline, diesel oil, heavy oil and carbonization gas.But LFC distillation process is complicated, and equipment is many, and cost is high; Self-produced low-heat value gas is difficult to meet technique needs heat, needs outer concurrent heating amount (supplying outside 30%); Gas outlet temperature is high, and heat-carrying gas consumption is large, and abundant not to the pyrolytic gas making of feed coal.For problems of the prior art, the present inventor explores and research through a large amount of, propose one fast pyrogenation and catalytic pyrolysis technology are merged mutually, oily pyrolytic process is put forward in pyrolytic gas making and the pyrolysis that can realize small-particle pyrolysis material, this technique can significantly improve the yield of pyrolysis gas and obtain a certain amount of pyrolysis oil, by adding catalyzer in pyrolysis reactor internal spray, catalyzer can be made to mix with pyrolysis material, being conducive to improving catalytic efficiency.And this technique adopts heat accumulation type radiant tube heating technique, without the need to gas, solid thermal barrier heating, simplify system process while improve the thermo-efficiency of reactor, there is important social benefit, economic benefit and environmental benefit.
In view of this, the invention provides a kind of pyrolysis plant.According to embodiments of the invention, this equipment comprises: pyrolysis hopper; The first feeding unit be connected with pyrolysis hopper; Pyrolysis reactor, it has gas-oil mixture outlet, the import of pyrolysis material and semicoke outlet, and the import of pyrolysis material is connected with the first feeding unit; Catalyst-adding device; Export with gas-oil mixture the condensate recycling device that is connected and export with semicoke the semicoke transfer roller be connected; Wherein, catalyst-adding device comprises: catalyst hooper; The catalyzer be connected with catalyst hooper is responsible for; With catalyzer be responsible for be connected and through pyrolysis reactor wall and extend to the catalyzer arm of the inside of pyrolysis reactor; Be positioned at pyrolysis reactor inside, and be arranged at least one the catalyst ejector part on catalyzer arm, and be responsible for catalyzer the carrier gas be connected and send part.
Contriver finds, simple according to this equipment reaction system architecture of the embodiment of the present invention, easy to operate, and catalyse pyrolysis is combined with fast pyrogenation, substantially increase carbonization gas (or claiming combustible gas or pyrolysis gas) productive rate, there is enough gas for the production of natural gas liquids (LNG) or liquefied petroleum gas (LPG) (LPG), good in economic efficiency, in addition, this equipment adds catalyzer by catalyst ejector part in pyrolysis reactor, catalyzer can be mixed equably with pyrolysis material in pyrolysis reactor, be conducive to improving catalytic efficiency.
According to embodiments of the invention, catalyzer arm is that multiple and along catalyzer supervisor length direction is arranged parallel to each other.
According to embodiments of the invention, catalyst ejector part comprises catalyzer jet pipe and is arranged on the nozzle on catalyzer jet pipe, and nozzle is provided with variable valve.
According to embodiments of the invention, pyrolysis reactor internal layout has multilayer heat accumulation type radiant tube, and catalyzer arm is arranged on the interlayer of heat accumulation type radiant tube.
According to embodiments of the invention, the end that part is connected to catalyzer supervisor is sent in carrier gas, and preferred carrier gas is sent part and removably connected or be soldered to catalyzer supervisor
According to embodiments of the invention, this pyrolysis plant may further include: loading hopper; The second feeding unit be connected with loading hopper; The drying installation be connected with heat accumulation type radiant tube with the second feeding unit respectively; The gas-solid separating device be connected with pyrolysis hopper with drying installation respectively; The exhaust gas cleaner be connected with gas-solid separating device.
According to embodiments of the invention, this pyrolysis plant may further include: the vapourizing furnace be connected with heat accumulation type radiant tube with semicoke transfer roller respectively.
In another aspect of the present invention, the invention provides a kind of method utilizing foregoing equipment to carry out pyrolysis.According to embodiments of the invention, the method comprises: pyrolysis material and catalyzer are added in pyrolysis reactor by the first feeding unit and catalyst-adding device and carry out pyrolytic reaction by (1) respectively, obtain gas-oil mixture and semicoke, wherein, utilize carrier gas to send part by carrier gas being blown into catalyzer supervisor, thus catalyzer is joined in pyrolysis reactor; (2) utilize condensate recycling device to carry out condensation process to gas-oil mixture, obtain pyrolytic tar and pyrolysis gas; (3) utilize semicoke transfer roller that semicoke is exported pyrolysis reactor.The method can process the pyrolysis material that granularity is below 2mm, raw material availability is high, be suitable for promoting, and catalyse pyrolysis is combined with fast pyrogenation, substantially increase the yield of carbonization gas, and obtain a certain amount of pyrolysis oil, good in economic efficiency, and add catalyzer by catalyst ejector part and catalyzer can be sprayed in the pyrolysis bed of material equably, catalyzer and pyrolysis material are mixed, improves catalytic efficiency.
According to embodiments of the invention, carrier gas is rare gas element, preferably nitrogen.
According to embodiments of the invention, the granularity of pyrolysis material is not more than 2 millimeters, and the granularity of catalyzer is not more than 0.5 millimeter.
The present invention at least has following beneficial effect:
1) take heat accumulation type radiant tube down-flow fluidized bed using ECT technique, reactive system structure is simple, and easy to operate, uniformity of temperature profile, heats is good.
2) can process the pyrolysis material that granularity is below 2mm, raw material availability is high, is suitable for promoting.
3) adopt catalyst fast pyrogenation, catalyse pyrolysis combines with fast pyrogenation, substantially increases the yield of carbonization gas, and obtains a certain amount of pyrolytic tar, good in economic efficiency.
4) when adopting catalyzer to carry out catalysis fast pyrogenation to coal, total carbonization gas productive rate is all higher than aluminium rice steamer method carbonization gas productive rate, and most high yield tolerance during catalysis fast pyrogenation is 150% of aluminium rice steamer method gas production rate.
5) around heat accumulation type radiant tube, be furnished with catalyzer ejection passage, catalyzer is sprayed in the pyrolysis bed of material equably by catalyzer ejection passage, makes pyrolysis material and catalyst mix evenly, is conducive to improving catalytic efficiency.
Accompanying drawing explanation
Fig. 1 shows the structural representation of the pyrolysis plant according to the embodiment of the present invention;
Fig. 2 shows the structural representation of the pyrolysis plant according to the embodiment of the present invention;
Fig. 3 shows the structural representation of the pyrolysis plant according to the embodiment of the present invention;
Fig. 4 shows the structural representation of the pyrolysis plant according to the embodiment of the present invention;
Fig. 5 shows the structural representation of the pyrolysis plant according to the embodiment of the present invention.
Embodiment
Embodiments of the invention are described below in detail.Embodiment described below is exemplary, only for explaining the present invention, and can not be interpreted as limitation of the present invention.Unreceipted concrete technology or condition in embodiment, according to the technology described by the document in this area or condition or carry out according to product description.Agents useful for same or the unreceipted production firm person of instrument, being can by the conventional products of commercial acquisition.
In describing the invention, it is to be appreciated that term " first ", " second " only for describing object, and can not be interpreted as instruction or hint relative importance or the implicit quantity indicating indicated technical characteristic.Thus, be limited with " first ", the feature of " second " can express or impliedly comprise one or more these features.In describing the invention, the implication of " multiple " is two or more, unless otherwise expressly limited specifically.
In the present invention, unless otherwise clearly defined and limited, the term such as term " installation ", " being connected ", " connection ", " fixing " should be interpreted broadly, and such as, can be fixedly connected with, also can be removably connect, or integral; Can be mechanical connection, also can be electrical connection; Can be directly be connected, also indirectly can be connected by intermediary, can be the connection of two element internals or the interaction relationship of two elements.For the ordinary skill in the art, above-mentioned term concrete meaning in the present invention can be understood as the case may be.
The invention provides a kind of pyrolysis plant.According to embodiments of the invention, with reference to Fig. 1, this equipment comprises: pyrolysis hopper 1; The first feeding unit 2 be connected with pyrolysis hopper 1; There is gas-oil mixture outlet 310, pyrolysis material import 320 and semicoke outlet 330, and the pyrolysis reactor 3 that pyrolysis material import 320 is connected with the first feeding unit 2; Catalyst-adding device 4, export 310 condensate recycling devices be connected 5 with gas-oil mixture and export the 330 semicoke transfer rollers 6 be connected with semicoke, wherein, catalyst-adding device 4 comprises: catalyst hooper 410; The catalyzer be connected with catalyst hooper 410 is responsible for 420; With catalyzer be responsible for 420 be connected and through pyrolysis reactor 3 wall and extend to the catalyzer arm 430 of pyrolysis reactor 3 inside; Be positioned at pyrolysis reactor 3 inner, and the catalyst ejector part 440 be arranged on catalyzer arm 430 and be responsible for 420 carrier gas be connected with catalyzer and send part (not shown).Contriver finds, simple according to this equipment reaction system architecture of the embodiment of the present invention, easy to operate, and catalyse pyrolysis is combined with fast pyrogenation, substantially increase carbonization gas (or claiming combustible gas or pyrolysis gas) productive rate, there is enough gas for the production of natural gas liquids (LNG) or liquefied petroleum gas (LPG) (LPG), good in economic efficiency, in addition, this equipment adds catalyzer by catalyst ejector part in pyrolysis reactor, catalyzer can be mixed equably with pyrolysis material in pyrolysis reactor, be conducive to improving catalytic efficiency.
According to embodiments of the invention, the concrete kind and the particle diameter that are applicable to the pyrolysis material of this equipment are not particularly limited, according to embodiments of the invention, pyrolysis material can be coal, rubbish, mud etc., pyrolysis material can be block pyrolysis material also can be small-particle pyrolysis material, in preferred embodiments more of the present invention, the particle diameter of the pyrolysis material that this equipment adopts can be not more than 2 millimeters, thus, small particles material can be made full use of, resource utilization is high, and can solve the problem of bulk deposition contaminate environment.
According to embodiments of the invention, the kind of the catalyzer of employing, particle diameter and consumption are not particularly limited, and those skilled in the art can select as required flexibly.In some embodiments of the invention, this equipment is used for pyrolysis fine coal, and the catalyzer that pyrolysis fine coal adopts can be at least one in iron, calcium oxide and sodium carbonate; The particle diameter of catalyzer can for being not more than 0.5 millimeter; The consumption of catalyzer can be 1% ~ 15% of pyrolysis material total mass.Thus, catalytic efficiency is higher, puies forward oily degree higher to the pyrolysis of pyrolysis material, pyrolysis oil and pyrolysis gas yield higher.
According to embodiments of the invention, catalyzer arm 430 can extend to the central position of pyrolysis reactor.Thus, catalyzer is conducive to and pyrolysis material mixes.And catalyzer arm 430 can be that multiple and along catalyzer supervisor 420 length direction is arranged parallel to each other.Thus, be conducive to catalyzer and be uniformly distributed in pyrolysis reactor 3, and then improve catalytic efficiency.
According to embodiments of the invention, catalyst-adding device 4 can comprise 10-25 layer catalyst ejector part.Thus, be conducive to catalyzer and be evenly distributed at pyrolysis reactor 3, improve catalytic efficiency.According to embodiments of the invention, catalyst ejector part 440 can comprise catalyzer jet pipe and be arranged on the nozzle on catalyzer jet pipe, thus, catalyzer can through catalyzer jet pipe under the effect of carrier gas, and by nozzle ejection in the pyrolysis bed of material, further, nozzle can also be provided with variable valve, be convenient to the add-on accurately controlling catalyzer thus.
According to embodiments of the invention, the quantity of catalyst ejector part 440 is not particularly limited, and those skilled in the art can set as required.In an embodiment of the present invention, each catalyzer arm 430 is provided with multiple catalyst ejector part 440, it can be provided with 4-15 nozzle.Thus, be conducive to catalyzer and pyrolysis material mixes, improve catalytic efficiency.
According to embodiments of the invention, the mode of connection that catalyzer arm 430 and catalyzer be responsible fors 420 is not particularly limited, and includes but not limited to removably or is connected to welding catalyzer and be responsible for.Ability and technician can select according to actual operating conditions.
According to embodiments of the invention, the end that part can be connected to catalyzer supervisor is sent in carrier gas, and concrete mode of connection is not particularly limited, and can removably connect or be soldered to catalyzer supervisor.Thus, be convenient to carrier gas and send part work, be conducive to increasing work efficiency.
According to embodiments of the invention, the concrete kind of the first pay-off 2 is not particularly limited, as long as the pyrolysis material in pyrolysis hopper 1 can be delivered in pyrolysis reactor 3 effectively.In some embodiments of the invention, the first pay-off 2 can be star feeder or feed screw, and under preferable case, the first pay-off 2 can be feed screw.Thereby, it is possible to realize the Automatic Conveying to hot feed, operational throughput is controlled, and device structure is simple, easy to operate.
According to embodiments of the invention, with reference to Fig. 2, pyrolysis reactor 3 internal layout has multilayer heat accumulation type radiant tube 340, and catalyzer arm 430 is arranged on the interlayer of heat accumulation type radiant tube 340.Specifically, vertically heat accumulation type radiant tube 340 and catalyzer jet pipe 440 alternating parallel distribute.Every layer of heat accumulation type radiant tube 340 can comprise multiple heat accumulation type radiant tube 340 parallel to each other and spaced apart in the horizontal direction.According to embodiments of the invention, heat accumulation type radiant tube 340 can be effective to heat material (pyrolysis material and catalyzer), it is made to carry out pyrolytic reaction, particularly, combustible gas and air can be passed in heat accumulation type radiant tube 340, make the heating function of combustible gas burning realization to material.This equipment adopts heat accumulation type radiant tube heating technique, without the need to gas, solid thermal barrier heating, pyrolysis gas can not be diluted, and calorific value is high, and uniformity of temperature profile in pyrolysis reactor, surface temperature difference is little, funnel temperature is low, and thermo-efficiency is high, simplifies system process while improve the thermo-efficiency of pyrolysis reactor, reactive system structure is simple, easy to operate.
According to embodiments of the invention, in pyrolysis reactor 3, material moves from top to bottom, and material scattering can make it be uniformly distributed by the heat accumulation type radiant tube 340 arranged in pyrolysis reactor 3.Meanwhile, catalyzer is sprayed in the pyrolysis bed of material by catalyst ejector part 440 equably, and make both Homogeneous phase mixing, catalytic efficiency is higher.According to embodiments of the invention, the shape of heat accumulation type radiant tube 340 is not particularly limited, and in some embodiments of the invention, can be cylindrical, be conducive to breaing up of material thus, realizes dispersed in pyrolysis reactor 3 of mixture.In addition, heat accumulation type radiant tube 340 can for the unidirectional heat accumulation type radiant tube be evenly arranged, the temperature of tube wall can control at 450 ~ 750 degree Celsius range by gas control valve, heat accumulation type radiant tube 340 can take the combustion system of regularly commutation, the surface temperature difference of single heat accumulation type radiant tube 340 is made to only have 30 degrees centigrade, there is no district of localized hyperthermia, thus, be conducive to improving thermo-efficiency.
According to embodiments of the invention, with reference to Fig. 3, this pyrolysis plant may further include: loading hopper 7; The second feeding unit 8 be connected with loading hopper 7; The drying installation 9 be connected with heat accumulation type radiant tube 340 with the second feeding unit 8 respectively; The gas-solid separating device 10 be connected with pyrolysis hopper 1 with drying installation 9 respectively; The exhaust gas cleaner 11 be connected with gas-solid separating device 10.Thus, pyrolysis material in loading hopper 7 can be added in drying installation 9 by the second feeding unit 8, in drying installation 9, pyrolysis material carries out drying under the effect of the flue gas (temperature is about 150 ~ 300 degrees Celsius) from heat accumulation type radiant tube 340, then the mixture of dried pyrolysis material and flue gas enters gas-solid separating device 10, the flue gas (temperature is about 70 ~ 150 degrees Celsius) being separated acquisition enters in exhaust gas cleaner 11 and carries out purifying treatment, to realize qualified discharge, being separated the pyrolysis material obtained is delivered in pyrolysis hopper 1, for carrying out pyrolytic reaction.
According to embodiments of the invention, the concrete kind of the second pay-off 8 is not particularly limited, as long as be applicable to the pyrolysis material in loading hopper 7 to be delivered in drying installation 9.In some embodiments of the invention, the second pay-off 8 can be star feeder or feed screw, and under preferable case, the second pay-off 8 can be feed screw.Thereby, it is possible to realize the Automatic Conveying to pyrolysis material, and operational throughput is controlled, and device structure is simple, easy to operate.
According to embodiments of the invention, the concrete kind of drying installation 9 is not particularly limited, as long as the function of the drying that can realize pyrolysis material and preheating.In some embodiments of the invention, drying installation 9 can be riser tube moisture eliminator, and thus, pyrolysis material carries out drying and lifting under the effect of flue gas, and the mixture of dried pyrolysis material and flue gas discharges riser tube moisture eliminator, is conducive to subsequent step and carries out.In drying installation 9, while drying is carried out to pyrolysis material, also achieve the function of preheating, be conducive to the speed and the efficiency that improve follow-up pyrolytic reaction, and the flue gas adopting heat accumulation type radiant tube 340 to discharge carries out drying and preheating to pyrolysis material, achieve the comprehensive utilization of heat energy, effectively reduce energy consumption, reach the object of energy-conserving and environment-protective.
According to embodiments of the invention, the concrete kind of gas-solid separating device 10 is not particularly limited, as long as pyrolysis material can be separated with flue gas.In some embodiments of the invention, gas-solid separating device 10 can be cyclonic separator, can be separated with flue gas by pyrolysis material quickly and efficiently thus, and good separating effect, simple to operation, cost is lower.
According to embodiments of the invention, blower fan 12 can also be provided with further between gas-solid separating device 10 and exhaust gas cleaner 11, the flue gas being separated acquisition in gas-solid separating device 10 can be delivered in exhaust gas cleaner 11 by blower fan 12 quickly and efficiently, is conducive to increasing work efficiency.
According to embodiments of the invention, this pyrolysis plant can also be provided with the chimney 13 be connected with exhaust gas cleaner 11, and the flue gas after exhaust gas cleaner 11 purifying treatment is emptying through chimney, thus, is conducive to protection of the environment, decreasing pollution.
According to embodiments of the invention, with reference to Fig. 4, this pyrolysis plant may further include: be connected with heat accumulation type radiant tube with semicoke transfer roller 6 respectively 340 vapourizing furnace 14.Thus, semicoke transfer roller 6 can be utilized to be delivered in vapourizing furnace 14 by obtaining semicoke in pyrolysis reactor 3, gasification process is carried out to semicoke, to obtain combustible gas and lime-ash, the combustible gas obtained can pass in heat accumulation type radiant tube 340, in heat accumulation type radiant tube 340, pass into air by blower fan 15 simultaneously, combustible gas is burnt the material in pyrolysis reactor 3 is heated.Thus, can utilize fully semicoke, not cause waste, good economy performance.
According to embodiments of the invention, the concrete kind of semicoke transfer roller 6 is not particularly limited, and includes but not limited to star or feed screw, and under preferable case, semicoke transfer roller 6 can be feed screw.Thereby, it is possible to realize the Automatic Conveying to semicoke, and operational throughput is controlled, and device structure is simple, easy to operate.
According to embodiments of the invention, with reference to Fig. 5, this pyrolysis plant comprise further export 310 respectively with gas-oil mixture, gas-solid separating device 15 that condensate recycling device 5 is connected with semicoke transfer roller 6, solid particulate for carrying in gas-oil mixture is separated, and be delivered to half-angle transfer roller 6 by being separated the solid particulate obtained, be delivered to condensate recycling device 5 by being separated the gas-oil mixture obtained.According to embodiments of the invention, gas-solid separating device 15 can be at least one, when gas-solid separating device 15 is multiple, be connected in series between each gas-solid separating device 15, and the concrete kind of gas-solid separating device 15 is also not particularly limited, as long as the solid particulate in gas-oil mixture effectively can be removed, such as, include but not limited to cyclonic separator.
According to embodiments of the invention, with reference to Fig. 5, this pyrolysis plant can also comprise the fuel cartridge 16 be connected with condensate recycling device 5, reclaims for storing condensate recycling device 5 pyrolysis gas obtained, further, the pyrolysis gas obtained can be further used for preparing LNG or LNP.Contriver finds, utilizes this equipment can significantly improve the yield of pyrolysis gas, has enough gas for the production of natural gas liquids (LNG) or liquefied petroleum gas (LPG) (LPG), good in economic efficiency.
In another aspect of the present invention, the invention provides a kind of method utilizing foregoing equipment to carry out pyrolysis.According to embodiments of the invention, the method can comprise the following steps:
(1) respectively pyrolysis material and catalyzer are added in pyrolysis reactor by the import of pyrolysis material and catalyst-adding device and carry out pyrolytic reaction, obtain gas-oil mixture and semicoke, wherein, utilize carrier gas to send part by carrier gas being blown into catalyzer supervisor, thus catalyzer is joined in pyrolysis reactor.
According to embodiments of the invention, the particle diameter of pyrolysis material is not particularly limited, can be that block pyrolysis material also can for small-particle pyrolysis material, in preferred embodiments more of the present invention, the particle diameter of pyrolysis material can be not more than 2 millimeters, thus, can make full use of small particles material, resource utilization is high, and can solve the problem of bulk deposition contaminate environment.According to embodiments of the invention, the concrete kind of pyrolysis material is also not particularly limited, as long as be suitable for the material adopting pyrolysis way process.In some embodiments of the invention, pyrolysis material can be coal, rubbish, mud etc.Thus, the method suitability is strong, has wide range of applications.
According to embodiments of the invention, the kind of the catalyzer of employing, particle diameter and consumption are not particularly limited, and those skilled in the art can select as required flexibly.In some embodiments of the invention, the catalyzer of pyrolyzing coal can be at least one in iron, calcium oxide and sodium carbonate; The particle diameter of catalyzer can for being not more than 0.5 millimeter; The consumption of catalyzer can be 1% ~ 15% of the total mass of feed coal.Thus, catalytic efficiency is higher, puies forward oily degree higher to the pyrolysis of feed coal, pyrolysis oil and pyrolysis gas yield higher.
According to embodiments of the invention, the temperature of pyrolytic reaction can be carried out under 500 ~ 600 degrees Celsius, particularly, the temperature that can control heat accumulation type radiant tube tube wall by gas valve is 450 ~ 750 degrees Celsius, pyrolysis material and catalyzer are heated to rapidly 500 ~ 600 degrees Celsius in pyrolysis reactor, complete pyrolytic process.
According to embodiments of the invention, before pyrolysis material is added pyrolysis hopper, drying treatment can also be carried out in advance to pyrolysis material, such as, the flue gas that heat accumulation type radiant tube can be adopted to discharge carries out drying and thermal pretreatment to pyrolysis material, thereby, it is possible to the moisture in removing pyrolysis material, be conducive to improving pyrolysis efficiency.According to embodiments of the invention, this method for pyrolysis can also comprise the step of dried flue gas being carried out to purifying treatment, to make tail gas qualified discharge, reduces environmental pollution.
(2) utilize condensate recycling device to carry out condensation process to gas-oil mixture, obtain pyrolytic tar and pyrolysis gas.
According to embodiments of the invention, in this step, the concrete mode that condensation is reclaimed does not receive special restriction, as long as pyrolysis oil effectively can be separated with pyrolysis gas, such as, includes but not limited to cooling, spray etc.Condensation is reclaimed the pyrolysis gas obtained and be may be used for preparing LNG or LPG.
(3) utilize semicoke transfer roller that semicoke is exported pyrolysis reactor.In process of production, continuously semicoke can be exported, the method can be carried out continuously.
According to embodiments of the invention, this method for pyrolysis can also comprise and utilizes vapourizing furnace to carry out the step of gasification process to semicoke, can fully utilize semicoke thus, good economy performance, the combustible gas that gasification obtains can pass into heat accumulation type radiant tube burning and heat for the material in pyrolysis reactor.
Contriver finds, the method can process the pyrolysis material of below 2mm, raw material availability is high, is suitable for promoting, and is combined with fast pyrogenation by catalyse pyrolysis, substantially increase the yield of carbonization gas, and obtain a certain amount of pyrolysis oil, good in economic efficiency, and add catalyzer by catalyzer ejection passage and catalyzer can be sprayed on equably in the pyrolysis bed of material, catalyzer and pyrolysis material are mixed, improves catalytic efficiency.
Referring to Fig. 5, for pyrolyzing coal, the specific works process of pyrolysis plant of the present invention and method is described in detail, specific as follows:
First, (can be lumped coal by feed coal, also can be fine coal, the particle diameter of preferred feedstock coal is not more than 2 millimeters) add in loading hopper 7, the second feeding unit 8 is utilized to add in riser tube moisture eliminator 9 by the feed coal be stored in loading hopper 1, the flue gas of 150 ~ 300 degrees Celsius of simultaneously discharging in heat accumulation type radiant tube 340 passes in riser tube moisture eliminator 9, feed coal carries out drying and lifting under the effect of flue gas, then the mixture of flue gas and feed coal discharges riser tube moisture eliminator 9, enter in gas-solid separating device (can be cyclonic separator) 10, be separated the flue gas (temperature is about 70 ~ 150 degrees Celsius) obtained and discharge the first gas-solid separating device 10, and exhaust gas cleaner 11 is entered under the effect of blower fan 13, carry out purifying treatment, purify the flue gas meeting emission standard obtained emptying through chimney 14, be separated the feed coal obtained in gas-solid separating device 10 and discharge gas-solid separating device 10, and enter in pyrolysis hopper 1, then the first pay-off 2 is utilized to add in pyrolysis reactor 3 by the feed coal be stored in pyrolysis material 1, catalyzer simultaneously in catalyst hooper 410 (includes but not limited to iron, calcium oxide, sodium carbonate etc.) send in carrier gas under the effect of the carrier gas (nitrogen) that part passes into successively through catalyzer supervisor 420, catalyzer arm 430 and catalyst ejector part 440 are evenly sprayed in raw material coal seam through nozzle, feed coal and catalyzer are 1:(0.01 ~ 0.15 according to mass ratio) ratio mixing, the mixture obtained moves from top to bottom in pyrolysis reactor 2, stop about 1 ~ 10 minute, break up with under heat effect at the heat accumulation type radiant tube 340 (pipe surface temperature is about 450 ~ 750 degrees Celsius) evenly arranged, mixture thermally equivalent is warming up to 500 ~ 600 degrees Celsius, complete pyrolytic reaction, obtain gas-oil mixture and semicoke, the gas-oil mixture obtained can export 310 discharge pyrolysis reactors 3 by gas-oil mixture, enter gas-solid separating device 15 (can be the cyclonic separator of two series connection), the semicoke carried in gas-oil mixture or other solid impurities separated and be delivered in vapourizing furnace 12 by semicoke transfer roller 6 and carry out gasification process, obtain combustible gas and pass into heat accumulation type radiant tube 340 for heating the material in pyrolysis reactor 3, the lime-ash that gasification process obtains discharges vapourizing furnace, gas-oil mixture after gas-solid separating device 15 is separated is transported to condensate recycling device 5, coal tar in gas-oil mixture is separated with pyrolysis gas, be separated the coal tar obtained to store for future use, the pyrolysis gas that separation obtains is transported to fuel cartridge 16 and stores under the effect of blower fan, can be further used for preparing LNG or LPG.
Embodiments of the invention are described below in detail.
Embodiment 1:
Utilize the heat storage type pyrolysis equipment shown in Fig. 5 to carry out pyrolysis processing to From Shenmu Coal, concrete steps are see the description of above general method, and the basic data of raw material, process operation parameter and material balance are in Table 1-table 3.
Table 1: From Shenmu Coal basic data
Table 2: process operation parameter
| Sequence number | Parameter name | Parameter value | Sequence number | Parameter name | Parameter value |
| 1 | Top radiator tube wall surface temperature | 625℃ | 6 | Reactor lower part temperature | 545℃ |
| 2 | Middle part radiator tube wall surface temperature | 625℃ | 7 | Reactor outlet temperature | 506℃ |
| 3 | Lower radiant tube wall surface temperature | 580℃ | 8 | Whirlwind temperature out | 485℃ |
| 4 | Reactor upper temp | 505℃ | 9 | Reactor pressure | 1.7Kpa |
| 5 | Reactor middle portion temperature | 540℃ |
Table 3: catalyst type and catalyzer usage ratio are on the impact of carbonization gas productive rate
In the description of this specification sheets, specific features, structure, material or feature that the description of reference term " embodiment ", " some embodiments ", " example ", " concrete example " or " some examples " etc. means to describe in conjunction with this embodiment or example are contained at least one embodiment of the present invention or example.In this manual, to the schematic representation of above-mentioned term not must for be identical embodiment or example.And the specific features of description, structure, material or feature can combine in one or more embodiment in office or example in an appropriate manner.In addition, when not conflicting, the feature of the different embodiment described in this specification sheets or example and different embodiment or example can carry out combining and combining by those skilled in the art.
Although illustrate and describe embodiments of the invention above, be understandable that, above-described embodiment is exemplary, can not be interpreted as limitation of the present invention, and those of ordinary skill in the art can change above-described embodiment within the scope of the invention, revises, replace and modification.
Claims (10)
1. a pyrolysis plant, is characterized in that, comprising:
Pyrolysis hopper;
First feeding unit, described first feeding unit is connected with described pyrolysis hopper;
Pyrolysis reactor, described pyrolysis reactor has gas-oil mixture outlet, the import of pyrolysis material and semicoke outlet, and the import of described pyrolysis material is connected with described first feeding unit;
Catalyst-adding device, described catalyst-adding device comprises:
Catalyst hooper;
Catalyzer is responsible for, and described catalyzer supervisor is connected with described catalyst hooper;
Catalyzer arm, described catalyzer arm is responsible for described catalyzer and is connected, described catalyzer arm through described pyrolysis reactor wall and extend to the inside of described pyrolysis reactor;
At least one catalyst ejector part, described catalyst ejector part is arranged on described catalyzer arm, and it is inner to be positioned at described pyrolysis reactor,
Part is sent in carrier gas, and described carrier gas is sent part and is responsible for described catalyzer and is connected,
Condensate recycling device, described condensate recycling device exports with described gas-oil mixture and is connected,
Semicoke transfer roller, described semicoke transfer roller exports with described semicoke and is connected.
2. equipment according to claim 1, is characterized in that, described catalyzer arm is multiple and the length direction be responsible for along described catalyzer is arranged parallel to each other.
3. equipment according to claim 1 and 2, is characterized in that, described catalyst ejector part comprises catalyzer jet pipe and is arranged on the nozzle on described catalyzer jet pipe, and described nozzle is provided with variable valve.
4. the equipment according to any one of claim 1-3, is characterized in that, described pyrolysis reactor internal layout has multilayer heat accumulation type radiant tube, and described catalyzer arm is arranged on the interlayer of described heat accumulation type radiant tube.
5. the equipment according to any one of claim 1-4, is characterized in that, the end that part is connected to described catalyzer supervisor is sent in described carrier gas, and preferred described carrier gas is sent part and removably connected or be soldered to described catalyzer supervisor.
6. the equipment according to any one of claim 1-5, is characterized in that, comprises further:
Loading hopper;
Second feeding unit, described second feeding unit is connected with described loading hopper;
Drying installation, described drying installation is connected with described heat accumulation type radiant tube with described second feeding unit respectively;
Gas-solid separating device, described gas-solid separating device is connected with described pyrolysis hopper with described drying installation respectively;
Exhaust gas cleaner, described exhaust gas cleaner is connected with described gas-solid separating device.
7. the equipment according to any one of claim 1-6, is characterized in that, comprises further:
Vapourizing furnace, described vapourizing furnace is connected with described heat accumulation type radiant tube with described semicoke transfer roller respectively.
8. utilize the equipment according to any one of claim 1-7 to carry out a method for pyrolysis, it is characterized in that, comprising:
(1) respectively pyrolysis material and catalyzer are added in pyrolysis reactor by the first feeding unit and catalyst-adding device and carry out pyrolytic reaction, obtain gas-oil mixture and semicoke, wherein, utilize carrier gas to send part by carrier gas being blown into catalyzer supervisor, thus catalyzer is joined in pyrolysis reactor;
(2) utilize condensate recycling device to carry out condensation process to described gas-oil mixture, obtain pyrolytic tar and pyrolysis gas;
(3) utilize described semicoke transfer roller that described semicoke is exported described pyrolysis reactor.
9. method according to claim 8, wherein said carrier gas is rare gas element, preferably nitrogen.
10. method according to claim 8 or claim 9, it is characterized in that, the granularity of described pyrolysis material is not more than 2 millimeters, and the granularity of described catalyzer is not more than 0.5 millimeter.
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