CN205328941U - Pyrolysis equipment - Google Patents
Pyrolysis equipment Download PDFInfo
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- CN205328941U CN205328941U CN201521004627.0U CN201521004627U CN205328941U CN 205328941 U CN205328941 U CN 205328941U CN 201521004627 U CN201521004627 U CN 201521004627U CN 205328941 U CN205328941 U CN 205328941U
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Abstract
The utility model provides a pyrolysis equipment, this equipment includes: the pyrolysis hopper, a feed arrangement who links to each other with the pyrolysis hopper, have oil -gas mixture export, the import of pyrolysis material and semi -coke outlet, and the pyrolytic reaction ware that links to each other with a feed arrangement is imported to the pyrolysis material, device, condensation recovery device who links to each other with the oil -gas mixture export and the semicoke conveyer that links to each other with semi -coke outlet are added to the catalyst. This equipment passes through catalyst blowout pipeline and adds the catalyst in to the pyrolytic reaction ware for the catalyst can mix in the pyrolytic reaction ware with the pyrolysis material uniformly, is favorable to improving catalysis efficiency.
Description
Technical field
This utility model relates to pyrolytic technique field, in particular it relates to pyrolysis plant。
Background technology
Natural gas, due to its clean environment firendly performance, is a kind of very valuable resource, and the energy resource structure of China is characterized as being " many coals, oil starvation, few gas ", and therefore coal liquifaction and coal gas are the outlets solving energy problem of China。Coal gas technological process is complicated, scale of investment is relatively big, and water resource consumption is big, becomes the bottleneck of restriction coal gas development。Coal low temperature distillation, product can comprehensively utilize (oil, gas, semicoke), can improve added value, increases economic benefit, can reduce again the environmental pollution that fire coal causes, it is believed that be the effective approach of coal high-efficiency clean utilization。Existing mainly have three river side's stoves of China, the hot solid carrier devolatilization technique of big work and a multistage rotary furnace pyrolytic process for industrial coal pyrolysis technique, external Wood stove, the strange three sections of stoves in Shandong, Kao Baisi stove and LFC retorting technique etc.。Some dry distilling type of furnaces are high to the Particle size requirements of raw material, can only pyrolysis lumped coal, cause small particles material to make full use of, resource utilization is not high and the problem of bulk deposition contaminated environment；The oily yield of some type of furnaces is relatively low, and with gas for heating carrier, causes condensate recovery system huge, and pyrogenation and carbonization gas is rushed rare, and gas heating value is low, it is difficult to the problems such as further comprehensive utilization；, then there is raw material and mix with heat carrier in the pyrolysis type of furnace of some solid thermal carriers, and heat carrier reheats the operations such as back-mixing, and technique is complex, equipment is more, and manufacturing cost and operating cost are high。Additionally, all to produce for the purpose of a large amount of tar in existing industry pyrolytic process, pyrolysis gas yield is less, or pyrolysis gas is burnt utilization by following cycle technique, and it is all inadequate to pyrolytic gas making and the liquefaction degree of coal that What is more。
Thus, current pyrolytic process of coal still haves much room for improvement。
Utility model content
One of technical problem that this utility model is intended to solve in correlation technique at least to a certain extent。For this, a purpose of the present utility model be in that to propose a kind of coal Particle size requirements is low, fast pyrogenation and catalytic pyrolysis technology are blended, pyrolysis oil yield is high or pyrolytic process without gas, solid heat carrier heating。
This utility model is based on the following discovery of inventor and completes:
The technical process of one of dry distillation of coal device conventional at present Germany strange three sections of stoves in Shandong is as follows: the qualified shove charge coal (particle diameter 20-80mm) shipped by standby coal workshop section is initially introduced in the coal bunker of furnace roof topmost, load the dryer section of gas retort then through charging aperture and auxiliary coal bin, be 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 upright pipes, and contact reverse with thermal current is heated at 500～850 DEG C and carries out middle low temperature distillation generates semicoke and dry distillation gas。At hypomere, the cooled circulating current of semicoke is cooled to 100～150 DEG C of discharges, and circulating air 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 combustion furnace, and some is sent directly into semicoke cooling section, and residual gas is sent outside。But, Germany's strange three sections of stoves in Shandong are high to granularity (20～80mm) and the coal quality requirements of feed coal, raw material availability is low, gas heat carrier heat supply, reduces the calorific value of carbonization gas, causes condensate recovery system and equipment huge, adopt wet quenching, the feature of environmental protection is poor, and semicoke must dry again, and it is abundant not that the pyrolysis of feed coal is carried oil。Another kind of conventional LFC distillation process utilizes heat smoke that oil shale particle raw material is dried, adopt the high-temperature flue gas that semicoke or carbonization gas burning produce that dry oil shale particle carries out heating indirectly and realize pyrolysis, obtain high-temperature oil gas and semicoke, high-temperature oil gas is filtered and after heat exchange, carries out fractional distillation 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 big, and the pyrolytic gas making of feed coal is abundant not。For problems of the prior art, inventor of the present utility model explores and research through a large amount of, propose one fast pyrogenation and catalytic pyrolysis technology to be blended, the pyrolytic gas making and the pyrolysis that are capable of little particle pyrolysis material put forward oily pyrolytic process, this technique can significantly improve the yield of pyrolysis gas and obtain a certain amount of pyrolysis oil, by adding catalyst in pyrolysis reactor internal spray, it is possible to make catalyst mix homogeneously with pyrolysis material, be conducive to improving catalytic efficiency。And this technique adopts heat accumulation type radiant tube heating technique, it is not necessary to gas, the heating of solid heat carrier, while improve the thermal efficiency of reactor, simplify system process, there is important social benefit, economic benefit and environmental benefit。
In view of this, this utility model provides a kind of pyrolysis plant。According to embodiment of the present utility model, this equipment includes: pyrolysis hopper；The first feed arrangement being connected with pyrolysis hopper；Pyrolysis reactor, it has gas mixture outlet, pyrolysis material import and semicoke outlet, and pyrolysis material import is connected with the first feed arrangement；Catalyst-adding device；The condensate recycling device being connected with gas mixture outlet and the semicoke conveyer being connected with semicoke outlet；Wherein, catalyst-adding device includes: catalyst hooper；The catalyst supervisor being connected with catalyst hooper；It is connected with catalyst supervisor and through the wall of pyrolysis reactor and extend to the catalyst arm of inside of pyrolysis reactor；It is positioned at inside pyrolysis reactor, and is arranged at least one the catalyst ejector part on catalyst arm, and the carrier gas being connected with catalyst supervisor delivers part。
Inventor have found that, this equipment reaction system structure according to this utility model embodiment is simple, easy to operate, and catalysis pyrolysis is combined with fast pyrogenation, substantially increase carbonization gas (or claiming combustible gas or pyrolysis gas) productivity, there is enough gas for producing liquefied natural gas (LNG) or liquefied petroleum gas (LPG), good in economic efficiency, additionally, this equipment adds catalyst by catalyst ejector part in pyrolysis reactor, catalyst can be mixed equably with pyrolysis material in pyrolysis reactor, be conducive to improving catalytic efficiency。
According to embodiment of the present utility model, catalyst arm is multiple and arranged parallel to each other along the length direction of catalyst supervisor。
According to embodiment of the present utility model, catalyst ejector part includes catalyst jet pipe and the nozzle being arranged on catalyst jet pipe, and is provided with adjustment valve on nozzle。
According to embodiment of the present utility model, being provided with multilamellar heat accumulation type radiant tube inside pyrolysis reactor, catalyst arm is arranged on the interlayer of heat accumulation type radiant tube。
According to embodiment of the present utility model, carrier gas delivers part and is connected to the end of catalyst supervisor, it is preferable that carrier gas delivery part is detachably connected or is soldered to catalyst supervisor
According to embodiment of the present utility model, this pyrolysis plant may further include: loading hopper；The second feed arrangement being connected with loading hopper；The drying device being connected with the second feed arrangement and heat accumulation type radiant tube respectively；The gas-solid separating device being connected with drying device and pyrolysis hopper respectively；The exhaust gas cleaner being connected with gas-solid separating device。
According to embodiment of the present utility model, this pyrolysis plant may further include: the gasification furnace being connected with semicoke conveyer and heat accumulation type radiant tube respectively。
This utility model at least has the advantages that
1) taking heat accumulation type radiant tube down-flow fluidized bed using ECT technique, response system simple in construction, easy to operate, uniformity of temperature profile, heats is good。
2) can processing the pyrolysis material that granularity is below 2mm, raw material availability is high, is suitable to promote。
3) adopting catalyst fast pyrogenation, catalysis 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) adopt catalyst when coal is carried out catalysis fast pyrogenation total carbonization gas productivity be above aluminum rice steamer method carbonization gas productivity, most high yield tolerance during catalysis fast pyrogenation is the 150% of aluminum rice steamer method gas production。
5) being furnished with catalyst ejection passage around heat accumulation type radiant tube, catalyst is sprayed in the pyrolysis bed of material by catalyst ejection passage equably so that pyrolysis material and catalyst mix are uniform, is conducive to improving catalytic efficiency。
Accompanying drawing explanation
Fig. 1 shows the structural representation of the pyrolysis plant according to this utility model embodiment；
Fig. 2 shows the structural representation of the pyrolysis plant according to this utility model embodiment；
Fig. 3 shows the structural representation of the pyrolysis plant according to this utility model embodiment；
Fig. 4 shows the structural representation of the pyrolysis plant according to this utility model embodiment；
Fig. 5 shows the structural representation of the pyrolysis plant according to this utility model embodiment。
Detailed description of the invention
Embodiment of the present utility model is described below in detail。The embodiments described below is illustrative of, and is only used for explaining this utility model, and it is not intended that to restriction of the present utility model。Unreceipted concrete technology or condition in embodiment, technology or condition described by the document in this area or carry out according to product description。Agents useful for same or the unreceipted production firm person of instrument, be can pass through city available from conventional products。
In description of the present utility model, it is to be understood that term " first ", " second " only for descriptive purposes, and it is not intended that instruction or hint relative importance or the implicit quantity indicating indicated technical characteristic。Thus, define " first ", the feature of " second " can express or implicitly include one or more these features。In description of the present utility model, " multiple " are meant that two or more, unless otherwise expressly limited specifically。
In this utility model, unless otherwise clearly defined and limited, the term such as term " installation ", " being connected ", " connection ", " fixing " should be interpreted broadly, for instance, it is possible to it is fixing connection, it is also possible to be removably connect, or integral；Can be mechanically connected, it is also possible to be electrical connection；Can be joined directly together, it is also possible to be indirectly connected to by intermediary, it is possible to be connection or the interaction relationship of two elements of two element internals。For the ordinary skill in the art, it is possible to understand above-mentioned term concrete meaning in this utility model as the case may be。
This utility model provides a kind of pyrolysis plant。According to embodiment of the present utility model, with reference to Fig. 1, this equipment includes: pyrolysis hopper 1；The first feed arrangement 2 being connected with pyrolysis hopper 1；There is gas 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 feed arrangement 2；Catalyst-adding device 4, exports 310 condensate recycling devices 5 being connected and exports the 330 semicoke conveyers 6 being connected with semicoke with gas mixture, and wherein, catalyst-adding device 4 includes: catalyst hooper 410；The catalyst supervisor 420 being connected with catalyst hooper 410；It is responsible for 420 be connected with catalyst and pass the wall of pyrolysis reactor 3 and extend to the catalyst arm 430 within pyrolysis reactor 3；It is positioned at pyrolysis reactor 3 internal, and is arranged on the catalyst ejector part 440 on catalyst arm 430 and is responsible for the 420 carrier gas delivery part (not shown)s being connected with catalyst。Inventor have found that, this equipment reaction system structure according to this utility model embodiment is simple, easy to operate, and catalysis pyrolysis is combined with fast pyrogenation, substantially increase carbonization gas (or claiming combustible gas or pyrolysis gas) productivity, there is enough gas for producing liquefied natural gas (LNG) or liquefied petroleum gas (LPG), good in economic efficiency, additionally, this equipment adds catalyst by catalyst ejector part in pyrolysis reactor, catalyst can be mixed equably with pyrolysis material in pyrolysis reactor, be conducive to improving catalytic efficiency。
According to embodiment of the present utility model, the concrete kind of pyrolysis material and particle diameter suitable in this equipment are not particularly limited, according to embodiment of the present utility model, pyrolysis material can be coal, rubbish, mud etc., pyrolysis material can be block pyrolysis material can also be little particle pyrolysis material, in preferred embodiments more of the present utility model, 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 the problem that can solve the problem that bulk deposition contaminated environment。
According to embodiment of the present utility model, the kind of the catalyst of employing, particle diameter and consumption are not particularly limited, and those skilled in the art can select as required flexibly。In embodiments more of the present utility model, this equipment is used for pyrolysis fine coal, and the catalyst that pyrolysis fine coal adopts can be at least one in ferrum, calcium oxide and sodium carbonate；The particle diameter of catalyst can for being not more than 0.5 millimeter；The consumption of catalyst can be the 1%～15% of pyrolysis material gross mass。Thus, catalytic efficiency is higher, the pyrolysis of pyrolysis material carries oil degree higher, and pyrolysis oil and pyrolysis gas yield are higher。
According to embodiment of the present utility model, catalyst arm 430 can extend to the center of pyrolysis reactor。Thus, catalyst and pyrolysis material mix homogeneously are conducive to。And catalyst arm 430 can be multiple and arranged parallel to each other along the length direction of catalyst supervisor 420。Thus, be conducive to catalyst to be uniformly distributed in pyrolysis reactor 3, and then improve catalytic efficiency。
According to embodiment of the present utility model, catalyst-adding device 4 can include 10-25 layer catalyst ejector part。Thus, be conducive to catalyst to be evenly distributed at pyrolysis reactor 3, improve catalytic efficiency。According to embodiment of the present utility model, catalyst ejector part 440 can include catalyst jet pipe and the nozzle being arranged on catalyst jet pipe, thus, catalyst can through catalyst jet pipe under the effect of carrier gas, and spray in the pyrolysis bed of material by nozzle, further, nozzle is also provided with regulate valve, is thus easy to accurately control the addition of catalyst。
According to embodiment of the present utility model, the quantity of catalyst ejector part 440 is not particularly limited, and those skilled in the art can set as required。In embodiment of the present utility model, each catalyst arm 430 is provided with multiple catalyst ejector part 440, it can be provided with 4-15 nozzle。Thus, be conducive to catalyst and pyrolysis material mix homogeneously, improve catalytic efficiency。
According to embodiment of the present utility model, the connected mode that catalyst arm 430 is responsible for 420 with catalyst is not particularly limited, and includes but not limited to removably or be connected to catalyst supervisor with welding。Ability and technical staff can select according to actual operating conditions。
According to embodiment of the present utility model, carrier gas delivers part can be connected to the end of catalyst supervisor, and concrete connected mode is not particularly limited, it is possible to detachably connected or be soldered to catalyst supervisor。Thus, it is simple to carrier gas delivers part work, be conducive to improving work efficiency。
According to embodiment of the present utility model, the concrete kind of the first pay-off 2 is not particularly limited, as long as can be effectively delivered in pyrolysis reactor 3 by the pyrolysis material in pyrolysis hopper 1。In embodiments more of the present utility model, the first pay-off 2 can be star feeder or feed screw, it is preferable that in situation, and the first pay-off 2 can be feed screw。Thereby, it is possible to realize the Automatic Conveying to hot feed, conveying capacity is controlled, and device structure is simple, easy to operate。
According to embodiment of the present utility model, with reference to Fig. 2, pyrolysis reactor 3 is internal is provided with multilamellar heat accumulation type radiant tube 340, and catalyst arm 430 is arranged on the interlayer of heat accumulation type radiant tube 340。Specifically, vertically heat accumulation type radiant tube 340 and the distribution of catalyst jet pipe 440 alternating parallel。Every layer of heat accumulation type radiant tube 340 can include the heat accumulation type radiant tube 340 of multiple parallel to each other and horizontally spaced distribution。According to embodiment of the present utility model, heat accumulation type radiant tube 340 can be effective to material (pyrolysis material and catalyst) is heated, it is made to carry out pyrolytic reaction, specifically, combustible gas and air can be passed in heat accumulation type radiant tube 340, make combustible gas burning realize the heating function to material。This equipment adopts heat accumulation type radiant tube heating technique, without gas, solid heat carrier heating, pyrolysis gas will not be diluted, and calorific value is high, and uniformity of temperature profile in pyrolysis reactor, surface temperature difference is little, exhaust gas temperature is low, and the thermal efficiency is high, simplifies system process while improve the thermal efficiency of pyrolysis reactor, response system simple in construction, easy to operate。
According to embodiment of the present utility model, in pyrolysis reactor 3, material moves from top to bottom, and material scattering can be made it be uniformly distributed by the heat accumulation type radiant tube 340 arranged in pyrolysis reactor 3。Meanwhile, catalyst is sprayed in the pyrolysis bed of material by catalyst ejector part 440 equably, makes both Homogeneous phase mixing, and catalytic efficiency is higher。According to embodiment of the present utility model, the shape of heat accumulation type radiant tube 340 is not particularly limited, in embodiments more of the present utility model, it is possible to for cylinder, is thus conducive to breaing up of material, it is achieved dispersed in pyrolysis reactor 3 of mixed material。Additionally, heat accumulation type radiant tube 340 can be the unidirectional heat accumulation type radiant tube being 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 making single heat accumulation type radiant tube 340 only has 30 degrees centigrade, there is no district of localized hyperthermia, thus, be conducive to improving the thermal efficiency。
According to embodiment of the present utility model, with reference to Fig. 3, this pyrolysis plant may further include: loading hopper 7；The second feed arrangement 8 being connected with loading hopper 7；The drying device 9 being connected with the second feed arrangement 8 and heat accumulation type radiant tube 340 respectively；The gas-solid separating device 10 being connected with drying device 9 and pyrolysis hopper 1 respectively；The exhaust gas cleaner 11 being connected with gas-solid separating device 10。Thus, the second feed arrangement 8 can be passed through the pyrolysis material in loading hopper 7 is added in drying device 9, in drying device 9, pyrolysis material is dried under the effect from the flue gas (temperature is about 150～300 degrees Celsius) of heat accumulation type radiant tube 340, then the mixture of dried pyrolysis material and flue gas enters gas-solid separating device 10, separate in flue gas (temperature is about 70～150 degrees Celsius) the entrance exhaust gas cleaner 11 obtained and carry out purified treatment, to realize qualified discharge, separate the pyrolysis material obtained and be delivered in pyrolysis hopper 1, for carrying out pyrolytic reaction。
According to embodiment of the present utility model, the concrete kind of the second pay-off 8 is not particularly limited, as long as being delivered in drying device 9 suitable in by the pyrolysis material loading hopper 7。In embodiments more of the present utility model, the second pay-off 8 can be star feeder or feed screw, it is preferable that in situation, and the second pay-off 8 can be feed screw。Thereby, it is possible to realize the Automatic Conveying to pyrolysis material, and conveying capacity is controlled, and device structure is simple, easy to operate。
According to embodiment of the present utility model, the concrete kind of drying device 9 is not particularly limited, as long as being capable of the function to the dry of pyrolysis material and preheating。In embodiments more of the present utility model, drying device 9 can be riser exsiccator, and thus, pyrolysis material is dried under the effect of flue gas and promotes, and the mixture of dried pyrolysis material and flue gas discharges riser exsiccator, is conducive to subsequent step to carry out。In drying device 9, while pyrolysis material is dried, also achieve the function of preheating, be conducive to improving speed and the efficiency of follow-up pyrolytic reaction, and adopt the flue gas that heat accumulation type radiant tube 340 is discharged that pyrolysis material is dried and is preheated, achieve the comprehensive utilization of heat energy, effectively reduce energy consumption, reach the purpose of energy-conserving and environment-protective。
According to embodiment of the present utility model, the concrete kind of gas-solid separating device 10 is not particularly limited, as long as can be separated with flue gas by pyrolysis material。In embodiments more of the present utility model, gas-solid separating device 10 can be cyclone separator, it is possible to pyrolysis material and flue gas are easily separated quickly and efficiently, and good separating effect, simple to operation, less costly。
According to embodiment of the present utility model, blower fan 12 can also be further provided with between gas-solid separating device 10 and exhaust gas cleaner 11, the flue gas separating 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 improving work efficiency。
According to embodiment of the present utility model, this pyrolysis plant is also provided with the chimney 13 being connected with exhaust gas cleaner 11, and the flue gas after exhaust gas cleaner 11 purified treatment empties through chimney, thus, is conducive to protection environment, reduces and pollute。
According to embodiment of the present utility model, with reference to Fig. 4, this pyrolysis plant may further include: be connected with semicoke conveyer 6 and heat accumulation type radiant tube respectively 340 gasification furnace 14。Thus, semicoke conveyer 6 can be utilized to be delivered in gasification furnace 14 by pyrolysis reactor 3 obtains semicoke, semicoke is carried out gasification process, 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, passed into air by blower fan 15 simultaneously, make combustible gas burning that the material in pyrolysis reactor 3 to be heated。Thus, it is possible to semicoke is utilized fully, do not cause waste, good economy performance。
According to embodiment of the present utility model, the concrete kind of semicoke conveyer 6 is not particularly limited, and includes but not limited to star or feed screw, it is preferable that in situation, and semicoke conveyer 6 can be feed screw。Thereby, it is possible to realize the Automatic Conveying to semicoke, and conveying capacity is controlled, and device structure is simple, easy to operate。
According to embodiment of the present utility model, with reference to Fig. 5, this pyrolysis plant farther includes the gas-solid separating device 15 being connected respectively with gas mixture outlet 310, condensate recycling device 5 and semicoke conveyer 6, solid particle for carrying in gas mixture separates, and it is delivered to half-angle conveyer 6 by separating the solid particle obtained, it is delivered to condensate recycling device 5 by separating the gas mixture obtained。According to embodiment of the present utility model, gas-solid separating device 15 can be at least one, when gas-solid separating device 15 is multiple, it is 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, if the solid particle that can effectively remove in gas mixture, for instance include but not limited to cyclone separator。
According to embodiment of the present utility model, with reference to Fig. 5, this pyrolysis plant can also include the fuel cartridge 16 being connected with condensate recycling device 5, the pyrolysis gas obtained for storing condensate recycling device 5 to reclaim, further, the pyrolysis gas obtained can be further used for preparation LNG or LNP。Inventor have found that, utilize this equipment can significantly improve the yield of pyrolysis gas have enough gas for producing liquefied natural gas (LNG) or liquefied petroleum gas (LPG), good in economic efficiency。
For the ease of understanding pyrolysis plant of the present utility model, of the present utility model in another, this utility model provides a kind of method utilizing foregoing equipment to carry out pyrolysis。According to embodiment of the present utility model, the method may comprise steps of:
(1) pyrolysis material and catalyst addition pyrolysis reactor will carry out pyrolytic reaction respectively by pyrolysis material import and catalyst-adding device, obtain gas mixture and semicoke, wherein, carrier gas is utilized to deliver part by carrier gas is blown into catalyst supervisor, thus being joined in pyrolysis reactor by catalyst。
According to embodiment of the present utility model, the particle diameter of pyrolysis material is not particularly limited, can be that block pyrolysis material can also for little particle pyrolysis material, in preferred embodiments more of the present utility model, the particle diameter of pyrolysis material can be not more than 2 millimeters, thus, it is possible to make full use of small particles material, resource utilization is high, and the problem that can solve the problem that bulk deposition contaminated environment。According to embodiment of the present utility model, the concrete kind of pyrolysis material is also not particularly limited, as long as be suitable for use with the material that pyrolysis way processes。In embodiments more of the present utility model, pyrolysis material can be coal, rubbish, mud etc.。Thus, the method suitability is strong, has wide range of applications。
According to embodiment of the present utility model, the kind of the catalyst of employing, particle diameter and consumption are not particularly limited, and those skilled in the art can select as required flexibly。In embodiments more of the present utility model, the catalyst of pyrolyzing coal can be at least one in ferrum, calcium oxide and sodium carbonate；The particle diameter of catalyst can for being not more than 0.5 millimeter；The consumption of catalyst can be the 1%～15% of the gross mass of feed coal。Thus, catalytic efficiency is higher, the pyrolysis of feed coal carries oil degree higher, and pyrolysis oil and pyrolysis gas yield are higher。
According to embodiment of the present utility model, the temperature of pyrolytic reaction can carry out under 500～600 degrees Celsius, specifically, it can be 450～750 degrees Celsius by the temperature of gas valve control heat accumulation type radiant tube tube wall, pyrolysis material and catalyst are heated to rapidly 500～600 degrees Celsius in pyrolysis reactor, complete pyrolytic process。
According to embodiment of the present utility model, before pyrolysis material is added pyrolysis hopper, in advance pyrolysis material can also be dried process, such as, can adopt the flue gas that heat accumulation type radiant tube is discharged that pyrolysis material is dried and the pre-heat treatment, thereby, it is possible to the moisture removed in pyrolysis material, be conducive to improving pyrolysis efficiency。According to embodiment of the present utility model, this method for pyrolysis can also include the step that dried flue gas carries out purified treatment, so that tail gas qualified discharge, reduces environmental pollution。
(2) utilize condensate recycling device that gas mixture is carried out condensation process, obtain pyrolytic tar and pyrolysis gas。
According to embodiment of the present utility model, in this step, the concrete mode that condensation is reclaimed does not receive special restriction, as long as can pyrolysis oil and pyrolysis gas be efficiently separated, for instance include but not limited to cooling, spray etc.。Condensation is reclaimed the pyrolysis gas obtained and be may be used for preparation LNG or LPG。
(3) utilize semicoke conveyer that semicoke is exported pyrolysis reactor。In process of production, it is possible to continuously semicoke is exported so that the method can continuously perform。
According to embodiment of the present utility model, this method for pyrolysis can also include utilizing gasification furnace that semicoke is carried out the step of gasification process, thus semicoke can be comprehensively utilized, good economy performance, the combustible gas that gasification obtains can pass into heat accumulation type radiant tube burning and be heated for the material in pyrolysis reactor。
Inventor have found that, the method can process the pyrolysis material of below 2mm, raw material availability is high, is suitable to promote, and catalysis 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 catalyst can be sprayed on equably in the pyrolysis bed of material by catalyst ejection passage addition catalyst, make catalyst and pyrolysis material mix homogeneously, improve catalytic efficiency。
Referring to Fig. 5, for pyrolyzing coal, the specific works process of pyrolysis plant of the present utility model and method is described in detail, specific as follows:
First, (can be lumped coal by feed coal, can also be fine coal, the particle diameter of preferred feedstock coal is not more than 2 millimeters) add in loading hopper 7, the second feed arrangement 8 is utilized to add in riser exsiccator 9 by the feed coal being stored in loading hopper 1, the flue gas of 150～300 degrees Celsius simultaneously discharged in heat accumulation type radiant tube 340 passes in riser exsiccator 9, feed coal is dried under the effect of flue gas and promotes, then the mixture of flue gas and feed coal discharges riser exsiccator 9, enter in gas-solid separating device (can be cyclone separator) 10, separate the flue gas (temperature is about 70～150 degrees Celsius) obtained and discharge the first gas-solid separating device 10, and under the effect of blower fan 13, enter exhaust gas cleaner 11, carry out purified treatment, purify the flue gas meeting discharge standard obtained to empty through chimney 14, gas-solid separating device 10 separates the feed coal obtained and discharges 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 being stored in pyrolysis material 1, catalyst in catalyst hooper 410 (includes but not limited to ferrum simultaneously, calcium oxide, sodium carbonate etc.) deliver under the effect of carrier gas (nitrogen) that part passes into catalyzed dose of supervisor 420 successively in carrier gas, catalyst arm 430 and catalyst ejector part 440 are uniformly sprayed in raw material coal seam through nozzle, feed coal and catalyst are 1:(0.01～0.15 according to mass ratio) ratio mixing, the mixed material obtained moves from top to bottom in pyrolysis reactor 2, stop about 1～10 minute, the heat accumulation type radiant tube 340 (tube wall temperature is about 450～750 degrees Celsius) being uniformly arranged break up with under heat effect, mixed material thermally equivalent is warming up to 500～600 degrees Celsius, complete pyrolytic reaction, obtain gas mixture and semicoke, the gas mixture obtained can pass through gas mixture outlet 310 discharge pyrolysis reactor 3, enter gas-solid separating device 15 (can be the cyclone separator of two series connection), the semicoke carried in gas mixture or other solid impurities are separated and be delivered in gasification furnace 12 and carried out gasification process by semicoke conveyer 6, obtain combustible gas and pass into heat accumulation type radiant tube 340 for the material in pyrolysis reactor 3 is heated, the lime-ash that gasification process obtains discharges gasification furnace, gas mixture after gas-solid separating device 15 separation is transported to condensate recycling device 5, coal tar in gas mixture and pyrolysis gas are easily separated, separate the coal tar obtained to store for future use, the pyrolysis gas that separation obtains is transported to fuel cartridge 16 under the effect of blower fan and stores, preparation LNG or LPG can be further used for。
Embodiment of the present utility model is described below in detail。
Embodiment 1:
Utilizing the heat storage type pyrolysis equipment shown in Fig. 5 that From Shenmu Coal is carried out pyrolysis processing, concrete steps are referring to the description of above conventional 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
Table 3: catalyst type and the impact on carbonization gas productivity of the catalyst usage ratio
In the description of this specification, specific features, structure, material or feature that the description of reference term " embodiment ", " some embodiments ", " example ", " concrete example " or " some examples " etc. means in conjunction with this embodiment or example describe are contained at least one embodiment of the present utility model or example。In this manual, the schematic representation of above-mentioned term is necessarily directed to identical embodiment or example。And, the specific features of description, structure, material or feature can combine in one or more embodiments in office or example in an appropriate manner。Additionally, when not conflicting, the feature of the different embodiments described in this specification or example and different embodiment or example can be carried out combining and combining by those skilled in the art。
Although above it has been shown and described that embodiment of the present utility model, it is understandable that, above-described embodiment is illustrative of, it is not intended that to restriction of the present utility model, above-described embodiment can be changed in scope of the present utility model, revises, replace and modification by those of ordinary skill in the art。
Claims (8)
1. a pyrolysis plant, it is characterised in that including:
Pyrolysis hopper；
First feed arrangement, described first feed arrangement is connected with described pyrolysis hopper；
Pyrolysis reactor, described pyrolysis reactor has gas mixture outlet, pyrolysis material import and semicoke outlet, and described pyrolysis material import is connected with described first feed arrangement；
Catalyst-adding device, described catalyst-adding device includes:
Catalyst hooper；
Catalyst is responsible for, and described catalyst supervisor be connected with described catalyst hooper；
Catalyst arm, described catalyst arm is connected with described catalyst supervisor, and described catalyst arm passes the wall of described pyrolysis reactor and extends to the inside of described pyrolysis reactor；
At least one catalyst ejector part, described catalyst ejector part is arranged on described catalyst arm, and is positioned at inside described pyrolysis reactor,
Carrier gas delivers part, and described carrier gas delivers part and is connected with described catalyst supervisor,
Condensate recycling device, described condensate recycling device is connected with the outlet of described gas mixture,
Semicoke conveyer, described semicoke conveyer is connected with the outlet of described semicoke。
2. equipment according to claim 1, it is characterised in that described catalyst arm is multiple and the length direction be responsible for along described catalyst is arranged parallel to each other。
3. equipment according to claim 1 and 2, it is characterised in that described catalyst ejector part includes catalyst jet pipe and the nozzle being arranged on described catalyst jet pipe, and described nozzle is provided with adjustment valve。
4. equipment according to claim 1, it is characterised in that being provided with multilamellar heat accumulation type radiant tube inside described pyrolysis reactor, described catalyst arm is arranged on the interlayer of described heat accumulation type radiant tube。
5. equipment according to claim 1, it is characterised in that described carrier gas delivers part and is connected to the end of described catalyst supervisor。
6. equipment according to claim 5, it is characterised in that described carrier gas delivery part is detachably connected or is soldered to described catalyst supervisor。
7. equipment according to claim 4, it is characterised in that farther include:
Loading hopper；
Second feed arrangement, described second feed arrangement is connected with described loading hopper；
Drying device, described drying device is connected with described second feed arrangement and described heat accumulation type radiant tube respectively；
Gas-solid separating device, described gas-solid separating device is connected with described drying device and described pyrolysis hopper respectively；
Exhaust gas cleaner, described exhaust gas cleaner is connected with described gas-solid separating device。
8. equipment according to claim 4, it is characterised in that farther include:
Gasification furnace, described gasification furnace is connected with described semicoke conveyer and described heat accumulation type radiant tube respectively。
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| CN201521004627.0U CN205328941U (en) | 2015-12-07 | 2015-12-07 | Pyrolysis equipment |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105368472A (en) * | 2015-12-07 | 2016-03-02 | 北京神雾环境能源科技集团股份有限公司 | Pyrolysis apparatus and method |
| CN106734994A (en) * | 2016-12-29 | 2017-05-31 | 龙南龙钇重稀土科技股份有限公司 | A kind of gas blowout pumpback formula suspending agent treatment mechanism |
| CN108057413A (en) * | 2018-02-07 | 2018-05-22 | 英丽化学（上海）股份有限公司 | A kind of methyl eight bromo ether based flame retardant prepares the solvent mixing arrangement entered |
| CN108456268A (en) * | 2018-02-07 | 2018-08-28 | 英丽化学（上海）股份有限公司 | It is a kind of to be dissolved in the device that dichloroethanes prepares brominated Polystyrene with polystyrene |
-
2015
- 2015-12-07 CN CN201521004627.0U patent/CN205328941U/en active Active
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105368472A (en) * | 2015-12-07 | 2016-03-02 | 北京神雾环境能源科技集团股份有限公司 | Pyrolysis apparatus and method |
| CN106734994A (en) * | 2016-12-29 | 2017-05-31 | 龙南龙钇重稀土科技股份有限公司 | A kind of gas blowout pumpback formula suspending agent treatment mechanism |
| CN108057413A (en) * | 2018-02-07 | 2018-05-22 | 英丽化学（上海）股份有限公司 | A kind of methyl eight bromo ether based flame retardant prepares the solvent mixing arrangement entered |
| CN108456268A (en) * | 2018-02-07 | 2018-08-28 | 英丽化学（上海）股份有限公司 | It is a kind of to be dissolved in the device that dichloroethanes prepares brominated Polystyrene with polystyrene |
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