CN103666501A - Pyrolysis system and pyrolysis method for solid carbonic material - Google Patents
Pyrolysis system and pyrolysis method for solid carbonic material Download PDFInfo
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- CN103666501A CN103666501A CN201210323648.3A CN201210323648A CN103666501A CN 103666501 A CN103666501 A CN 103666501A CN 201210323648 A CN201210323648 A CN 201210323648A CN 103666501 A CN103666501 A CN 103666501A
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Abstract
The invention relates to a pyrolysis system for a solid carbonic material. The pyrolysis system comprises a circulating fluid bed hearth, a first separator, a solid heat carrier channel and a pyrolysis channel, wherein the first separator is connected with a smoke outlet of a circulating fluid bed; a solid heat carrier flows inside the solid heat carrier channel in a fluidized state; the granular solid carbonic material containing a volatile component is added from the upper part, passes through the pyrolysis channel from top to bottom by using the gravity in a fluidized state, and generates pyrolysis reaction; the pyrolysis channel and the solid heat carrier channel are partitioned by a heat-conducting dividing wall; the solid heat carrier and the solid carbonic material inside the pyrolysis channel are subjected to heat exchange through the heat-conducting dividing wall; the solid carbonic material is heated and subjected to pyrolysis reaction; the solid heat carrier inlet of the solid heat carrier channel is communicated with a solid outlet of the first separator; and an overflow port is formed at the lateral wall of the solid heat carrier channel, and communicated with a material return opening of the hearth. The invention also relates to a pyrolysis method for the solid carbonic material.
Description
Technical field
The present invention relates to the pyrolysis of solid carbon material, relate in particular to particulate state containing pyrolysis system and the method for pyrolysis of the solid carbon material of volatile matter.
Background technology
It is current cascade utilization low-rank coal resource that coal generates coal gas, tar and semicoke by pyrolysis, obtains the higher value application approach of high added value product, and economic benefit and social benefit are remarkable.In recent years, resinous shale becomes the non-traditional hydrocarbon resources of universally acknowledged tool potentiality, because its oil length is generally 4%～20%, reaches as high as 30%, and therefore, except combustion power generation, mainly utilizing mode is destructive distillation oil refining.Resinous shale is after heating destructive distillation, and contained oil mother stock solution generates shale oil and carbonization gas and shale semicockes; Shale oil can be used as oil fuel, also can further process and produce vapour, diesel oil and chemical.Resinous shale is carried out to effective development and utilization, can alleviate the predicament that China lacks natural oil, reduce the dependence to Imported oil, safeguard national energy security, improve energy structure.In addition, contain a large amount of organic matters and combustiblecomponents in dewatered sludge, dewatered sludge pyrolysis processing can impel organism in mud to reduce, generation can be for the fuel of recycling, the calorific value of its pyrolytic tar is higher, can be used as energy utilization, can reach the quality of oil used in fuel with solar oil after mixing.
In pyrolytic process, heat and mass mode has remarkably influenced to the quality of pyrolysis product.For lump coal, it is ripe that pyrolytic technique has been tending towards, and mainly adopts fixed-bed pyrolysis technique, as the vertical retort on the ground such as northern Shensi, Inner Mongol, requires the granularity of coal larger.Along with the raising of coal mining mechanization degree, the fine coal output that granularity is less increases just year by year, present stage pulverized coal pyrolysis operational path more.According to the supply mode of pyrolytic reaction institute heat requirement, pyrolytic process can be divided into direct contact heat transfer and the large class of indirect contact heat exchanger two.
Direct contact heat transfer mode is mainly directly to mix with the coal for the treatment of pyrolysis by high-temperature gas or solid thermal carriers, material is heated up pyrolytic reaction occurs.The advantages such as it is high that direct contact heat transfer technology has heat transfer efficiency, and heating rate is fast.But in high-temperature gas thermal barrier technique, because carry secretly, mixing etc. makes to contain a large amount of inert components in coal gas, reduce caloric power of gas, tar dustiness increases, and reduces quality.In high-temp solid thermal barrier technique, the fine particle in thermal barrier enters in pyrolysis gas and tar, separation difficulty, and easily there is the problems such as line clogging.And the tarry vapours that pyrolysis of coal produces contacts with the direct of high-temperature heat carrier, and second pyrolysis easily occurs, and affects tar quality and productive rate.Meanwhile, in pyrogenous origin semicoke, because having sneaked into solid thermal carriers particle, its calorific value is reduced, affected the quality of semicoke.
Indirect heat exchange technology is to conduct heat to material by reactor heating outer walls such as external electric, high-temperature flue gas, high-temperature material, high-temperature thermal storage bodies, makes material skin to internal layer, conduct heat and heat up and the process of generation pyrolytic reaction successively.Indirect contact heat exchanger technology is not because sneaking into other thermal barrier, and the caloric power of gas of acquisition is higher, and in tar, dustiness is low, semicoke product inclusion-free, and quality is high.But because the heat conductivility of coal is poor, in indirect heat exchange pyrolytic process of coal, slow, the non-uniform temperature of material temperature rise rate, easily causes the problems such as pyrolysis time is long, tar yield is low, mink cell focus content height.
Summary of the invention
For solving the problem of at least one aspect of the prior art, the present invention is proposed.
Core inventive concept of the present invention (usining coal as example) is following aspect: adopt solid thermal carriers as the thermal source of pyrolysis, solid thermal carriers with treat that the coal of pyrolysis is indirect heat exchange, indirect heat exchange wall both sides are fluidization.Similarly to the prior art, coal adds from top one side of pyrolysis, from bottom, discharges, and by the gaseous state pyrolysis product self-fluidized type producing, thereby is preferably respectively from below to up moving-bed, Micro Fluid, these three kinds of states of fluidisation; As a side of thermal source unlike the prior art, adopt in fluidised solid thermal carriers.Wherein, gaseous state pyrolysis product comprises water vapour, the pyrolysis gas that pyrolysis of coal produces and is at high temperature the tar of gaseous state (be tarry vapours, be called for short oil gas).
Other inventive concept of the present invention (take coal as example) is also following aspect:
1, solid thermal carriers can be heated in solid thermal carriers passage, can be also to enter solid thermal carriers passage after being heated in advance again.For example, can adopt the mode of geseous fuel, liquid fuel or solid fuel ignition, heated inert particle; Or directly using solid fuel particle as solid thermal carriers, by the burning generation heat of himself.
2, pyrolysis oven bottom is lower than thermal barrier bed bottom, be that pyrolysis oven bottom exists one section not heated " releasing most section ", for extending the residence time of pyrolyzing coal, for residual volatile matter, disengage, and improve the adaptability of system, when ature of coal changes or when the granularity of coal changes, in order to guarantee that volatile matter discharges completely.
3, the fluidized-bed sidewall of thermal barrier can be provided with overflow port, when solid thermal carriers flow through from passage, in the mode of overflow, discharges, thereby keeps stable emulsion zone height, and the height of overflow port is at the emulsion zone of Particles In Fluidized Bed of Heat Carrier and the transition section between freeboard of fluidized bed.
4, the fine coal for the treatment of pyrolysis carries out sorting in advance, and the fine coal that particle diameter is too small is sent into hearth combustion, and using remaining fine coal as pyrolyzing coal, thereby reduce, is blended into the amounts of fine particles in pyrolysis product; Or, do not limit the particle diameter of the fine coal that the particle diameter that sorts out is less, but can meet the required heat of pyrolytic reaction with the amount burning heat release of the fine coal that sub-elects, be as the criterion, the fine coal particle diameter sub-electing may be than front a kind of larger under conceiving.
When the fine coal of 5, treating pyrolysis carries out sorting, can adopt dry-sorting integrated technique, in sorting, realize the dry of fine coal, enter hearth combustion together with the dry weary gas producing of the coal fine coal less with the particle diameter sub-electing.
According to a first aspect of the invention, proposed a kind of pyrolysis system for solid carbon material, having comprised: circulating fluidized bed burner hearth; The first separator being connected with the exhanst gas outlet of circulating fluidized bed; Solid thermal carriers passage, solid thermal carriers flow in described solid thermal carriers passage with fluidized state; Pyrolysis passage, particulate state adds from top containing the solid carbon material of volatile matter, utilize gravity from top to bottom with fluidized state by described pyrolysis passage, concurrent raw pyrolytic reaction, wherein: described pyrolysis passage and solid thermal carriers passage by heat conduction partition, separate and described solid thermal carriers and described pyrolysis passage in solid carbon material by the heat exchange of described heat conduction partition, solid carbon material is heated, occurs pyrolytic reaction; The solid thermal carriers entrance of described solid thermal carriers passage communicates with the solid outlet of described the first separator, and the sidewall of described solid thermal carriers passage is provided with overflow port, and described overflow port communicates with the returning charge mouth of burner hearth.
Optionally, described pyrolysis passage comprises many thermal decomposition tubes or a plurality of pyrolysis passage being arranged in described solid thermal carriers passage.
Optionally, described solid thermal carriers comprise that the preferable particle size scope joining in burner hearth or solid thermal carriers passage is the inert particle of 0-2mm.Further, at least a portion pyrolysis product from the outlet of described pyrolysis passage top is fed into burner hearth as fuel.Further, described at least a portion pyrolysis product comprises heavy tar and/or pyrolysis gas.Optionally, in described solid thermal carriers passage, add the fuel that is useful on heat solid thermal barrier.
Optionally, described solid carbon material is coal, resinous shale, dewatered sludge or biological particles.Further, the particle diameter of described solid carbon material is within the scope of 0-12mm.Optionally, described solid carbon material pyrolysis system also comprises: sorting subsystem, and the solid carbon material by particle diameter below 0.1mm removes; And transport subsystem, be suitable for carrying the particle diameter sub-elect from the sorting subsystem solid carbon material more than 0.1mm to pyrolysis passage.Optionally, described sorting subsystem comprises: fluid bed separation passage, fluidizing agent is introduced described sort channel and with fluidisation, is arranged in the solid carbon material of described sort channel from the bottom of described sort channel, the bottom of described sort channel is provided with large particle diameter solid carbon material relief outlet; The second separator, the entrance of described the second separator communicates with the outlet of the top of described sort channel, the pneumatic outlet of described the second separator is discharged solid carbon material and the fluidizing agent of particle diameter below 0.1mm, wherein: from described large particle diameter solid carbon material relief outlet with from the solid carbon material of the solid outlet of described the second separator, enter described transport subsystem.Optionally, in described fluid bed separation passage, be provided with dry heat unit, for the solid carbon material of drying fluidized-bed sort channel.Optionally, the pneumatic outlet of described the second separator communicates and thinks that burner hearth provides fuel with described burner hearth.
Optionally, described solid carbon material pyrolysis system also comprises solid carbon goods fluid sorting unit, the solid carbon material of discharging from the top outlet of sorting unit is transported to circulating fluidized bed burner hearth, and the solid carbon material of discharging from the lower part outlet of sorting unit is transported to described pyrolysis passage.Further, the described solid carbon material of discharging, be transported to burner hearth from the outlet of sorting unit top, the required heat of its combustion heating amount and pyrolysis passage matches.
Optionally, the solid thermal carriers freeboard of fluidized bed that described solid thermal carriers passage comprises solid thermal carriers emulsion zone and is positioned at described emulsion zone top; Solid carbon material in described pyrolysis passage has at least a part to be fluidized-bed state, and forms fluidized-bed bed surface, wherein, the bed surface of described solid thermal carriers emulsion zone substantially with described pyrolysis passage in fluidized-bed bed surface contour, or a little less than the latter.Further, described pyrolysis passage comprises pyrolysis section, heating zone from bottom to top, and the solid carbon material that is arranged in described pyrolysis section and heating zone is respectively Micro Fluid state and fluidized state.Further, the position of described pyrolysis section and heating zone and the position of described emulsion zone are roughly corresponding.Optionally, the position of described pyrolysis section is roughly corresponding with the position of described emulsion zone, and the position of described heating zone is roughly corresponding with the position of described freeboard of fluidized bed.
Optionally, described pyrolysis passage comprises from below to up releases most section, pyrolysis section, heating zone, and the solid carbon material of releasing most section, pyrolysis section and heating zone described in being arranged in is respectively moving-bed state, Micro Fluid state, fluidized state.Further, the position of described pyrolysis section and heating zone and the position of described emulsion zone are roughly corresponding.Further, the position of described pyrolysis section is roughly corresponding with the position of described emulsion zone, and the position of described heating zone is roughly corresponding with the position of described freeboard of fluidized bed.Optionally, described in, release most section of below that is arranged in described emulsion zone and do not form heat exchange with the solid thermal carriers of solid thermal carriers passage.
Optionally, described solid carbon material utilize the gaseous state pyrolysis product that produces in pyrolysis passage with the state of self-fluidized type by described pyrolysis passage.
Optionally, described solid carbon material utilize the gaseous state pyrolysis product producing in pyrolysis passage and the other fluidizing agent passing into from pyrolysis passage bottom with the state of fluidisation by described pyrolysis passage.Further, described other fluidizing agent is pyrolysis gas, hydrogen, methane or other non-oxidizing gas.
Optionally, the described pyrolysis system for solid carbon material also comprises: refrigerating unit, the solid product that discharge from pyrolysis passage after for the pyrolysis of cooling solid carbonaceous material the below that described refrigerating unit is arranged in described pyrolysis passage.
According to a second aspect of the invention, proposed a kind of method for pyrolysis of solid carbon material, comprised step: in solid thermal carriers channel bottom, passed into fluidizing agent, solid thermal carriers are flowed in solid thermal carriers passage with fluidized state, to utilizing in the separated pyrolysis passage of heat conduction partition and solid thermal carriers passage, supply with particulate state containing the solid carbon material of volatile matter, wherein, described solid carbon material utilize gravity from top to bottom with fluidized state by described pyrolysis passage, solid carbon material in described solid thermal carriers and described pyrolysis passage is by the heat exchange of heat conduction partition, solid carbon material is heated, there is pyrolytic reaction, wherein: described solid thermal carriers channel setting is in the circulation loop of circulating fluidized bed burner hearth outside, the solid thermal carriers entrance of described solid thermal carriers passage with and the solid outlet of the separator that is communicated with of burner hearth flue communicate, the sidewall of described solid thermal carriers passage is provided with overflow port, described overflow port communicates with the returning charge mouth of burner hearth.
Further, in aforesaid method, described solid thermal carriers comprise fuel pellet and solid-state products of combustion thereof.
Favourable, aforesaid method also comprises step: in burner hearth or solid thermal carriers passage, add the inert particle as solid thermal carriers.
Optionally, above method also can comprise step: provide solid carbon material, and the solid carbon material below 0.1mm removes by particle diameter to utilize a minute selection operation; And to supplying with the particle diameter that the sub-elects solid carbon material more than 0.1mm in pyrolysis passage.Favourable, aforesaid method also comprises step: the solid carbon material by particle diameter below 0.1mm is sent to stove chamber inner combustion.
Or optional, above method also can comprise step: solid carbon mass transport is arrived to solid carbon goods fluid sorting unit, the solid carbon material of discharging from the top outlet of sorting unit is transported to circulating fluidized bed burner hearth, and the solid carbon material of discharging from the lower part outlet of sorting unit is transported to described pyrolysis passage.Favourable, regulate and pass into the fluidized gas scale of construction of sorting unit, so that be transported to the combustion heating amount of the solid carbon material of burner hearth from sorting unit, the heat required with pyrolysis passage matches.
Utilize technical scheme of the present invention, the process that the heat release under two fluidized states is provided and has absorbed heat and combine, solid thermal carriers and pyrolysis passage all exist in fluidised interval, and intercouple by heat conduction partition; Under fluidized state, the large whirlpool of the low frequency body of random bubble formation makes particle occur radially to transport, just as stirring, effectively disturbance thermal boundary layer, improved the heat transfer coefficient of heat conduction partition both sides, therefore strengthened heat transfer; The more important thing is, mate mutually heat exchanger heat conduction wall both sides: pyrolysis side, particulate state containing the solid carbon material of volatile matter from top adds, by rapid heating, then there is pyrolytic reaction; Solid thermal carriers side, solid thermal carriers are in fluidized state, the emulsion zone of solid thermal carriers side is roughly corresponding with pyrolysis side heating zone and pyrolysis section, because of emulsion zone granule density high, heat transfer coefficient is large, can provide amount of heat to heating zone and pyrolysis section, well meet the needs of solid carbon material rapid heating and pyrolysis; And two upper lateral parts are all in freeboard of fluidized bed, granule density is low, heat exchange weakens, and excess Temperature while just in time avoiding gaseous state pyrolysis product to discharge from top, second pyrolysis occurs.Technical scheme of the present invention has not only been strengthened heat-transfer effect effectively, has also avoided hot ash in the technical scheme of direct mixed heat transfer to be blended into the situation in pyrolysis product.
Accompanying drawing explanation
Fig. 1 is according to the schematic diagram of the pyrolysis of coal system of the first embodiment of the present invention;
Fig. 2 is the schematic diagram of pyrolysis of coal system according to a second embodiment of the present invention;
Fig. 3 is the schematic diagram of the pyrolysis of coal system of a third embodiment in accordance with the invention;
Fig. 4 is the schematic diagram of the pyrolysis of coal system of a fourth embodiment in accordance with the invention;
Fig. 5 a is the schematic diagram of the layout between pyrolysis of coal passage according to an embodiment of the invention and solid thermal carriers passage, Fig. 5 b is for representing the height of pyrolysis of coal passage and the exemplary graph of the relation between the temperature of the coal in pyrolysis of coal passage, and Fig. 5 c is for representing the height of pyrolysis of coal passage and the exemplary graph of the relation between gaseous state pyrolysis product amount, relation between the gaseous state pyrolysis product amount that wherein each height location of the exemplary expression pyrolysis of coal of curve I passage and the coal of this At The Height discharge, the height of the exemplary expression pyrolysis of coal of curve II passage and the relation between gaseous state pyrolysis product semi-invariant,
Fig. 6 is pyrolysis of coal passage according to another embodiment of the invention and the schematic diagram of the layout between solid thermal carriers passage;
Fig. 7 is according to the schematic diagram of the layout between the pyrolysis of coal passage of an embodiment more of the present invention and solid thermal carriers passage;
Fig. 8 is pyrolysis of coal passage according to an alternative embodiment of the invention and the schematic diagram of the layout between solid thermal carriers passage;
Fig. 9 is pyrolysis of coal passage according to still another embodiment of the invention and the schematic diagram of the layout between solid thermal carriers passage.
Embodiment
Describe the embodiment of exemplary of the present invention below in detail, the example of embodiment is shown in the drawings, and wherein same or analogous label represents same or analogous element.The embodiment describing below with reference to accompanying drawing is exemplary, is intended to explain the present invention, and can not be interpreted as limitation of the present invention.
First, need to be pointed out that specially, although the present invention be take coal and has been described pyrolysis system and method for pyrolysis as concrete example, but this pyrolysis system and method for pyrolysis can also be applied to the particulate state such as resinous shale, dewatered sludge and biomass containing the pyrolysis of the solid carbon material (especially particle diameter is within the scope of 0-12mm) of volatile matter.
Below with reference to Fig. 1-3, describe according to the pyrolysis of coal system of exemplary embodiment of the present invention.
As shown in Fig. 1-3, described pyrolysis of coal system comprises: circulating fluidized bed burner hearth 50; The first separator 60 being connected with the exhanst gas outlet of circulating fluidized bed 50; Solid thermal carriers path 10, solid thermal carriers A flows in described solid thermal carriers path 10 with fluidized state; Pyrolysis of coal passage 20, particulate coal B adds from top, utilize gravity from top to bottom with fluidized state by described pyrolysis of coal passage 20, concurrent raw pyrolytic reaction, wherein: described pyrolysis of coal passage 20 separate by heat conduction partition 30 with solid thermal carriers path 10 and described solid thermal carriers A and described pyrolysis of coal passage in coal B by described heat conduction partition 30 heat exchange, coal B is heated, occurs pyrolytic reaction; The solid thermal carriers entrance 16 of described solid thermal carriers path 10 communicates with the solid outlet of described the first separator 60, and the sidewall of described solid thermal carriers passage is provided with overflow port 15, and described overflow port 15 communicates with the returning charge mouth 51 of burner hearth.
As shown in Fig. 1-3, treat that the coal of pyrolysis can be transported to pyrolysis of coal passage 20 by hopper 71 and the transfer roller 72 that is arranged in hopper below.
Pyrolysis of coal passage 20 can be single passage, as shown in Fig. 1,3, also can comprise the many thermal decomposition tubes or a plurality of pyrolysis passage that are arranged in described solid thermal carriers path 10, as shown in Figure 2.It is pointed out that many thermal decomposition tubes or a plurality of pyrolysis passage can communicate in the ingress for the treatment of pyrolyzing coal (or sharing same coal entrance), also can be independent of one another, for example by each self-corresponding hopper 71 and transfer roller 72, supply with pyrolyzing coal.
Solid thermal carriers A can be comprised of solid fuel and the solid-state products of combustion thereof of burning in burner hearth 50; At the former, do not exist or when quantity is few, also can add inert particle to burner hearth 50 or solid thermal carriers path 10, fine sand for example, as solid thermal carriers A, because improve the granule density in solid thermal carriers passage, can further strengthen to the heat transfer of pyrolysis of coal passage 20.The particle size range of preferred inert particle is 0-2mm.
As shown in Fig. 2,3, at least a portion pyrolysis product exporting from described pyrolysis of coal passage top can be fed into burner hearth as fuel.Favourable, described at least a portion pyrolysis product comprises heavy tar and/or pyrolysis gas.As shown in Fig. 2,3, from the pyrolysis product of pyrolysis of coal passage upper opening, be first passed into pulverized-coal collector 80.The solid outlet of pulverized-coal collector 80 is discharged separated coke powder, and this coke powder can also be discharged after overcooling.The pneumatic outlet of pulverized-coal collector 80 communicates with oil recovery system 90, in oil recovery system, realizes the separated of tar steam and pyrolysis gas, and pyrolysis gas and heavy tar can be passed in burner hearth as fuel, and light oil is collected as target product.Although in Fig. 2,3, pyrolysis gas and heavy tar are all passed in burner hearth and are burnt,, also can only pass into wherein a kind of or part and be passed in burner hearth.
Although do not illustrate,, also can in solid thermal carriers path 10, add the fuel for heat solid thermal barrier A.Accordingly, the fluidizing agent being passed in solid thermal carriers passage provides burning required oxygen.The air quantity of suitably controlling fluidized wind makes in solid thermal carriers path 10 still in burning or partial combustion state, to maintain the stable condition of high temperature as far as possible, thereby keep the heat transfer temperature difference between the solid thermal carriers A of heat conduction partition 30 1 sides and the coal B of the opposite side of heat conduction partition 30 to keep stable.This can greatly reduce the usage quantity of solid thermal carriers, thereby reduce, dynamically consumes, alleviates wearing and tearing.
The particle size range of the applicable solid carbon material of the present invention is mainly 0 ~ 12mm, but has the fine powder that particle diameter is less in this particle size range, and fine powder is easy to be carried by gaseous state pyrolysis product, finally can be blended in tar and be difficult to separation; Meanwhile, the coal grain larger with respect to particle diameter, in fine powder, water content is more, and this can produce too much water vapour and consume amount of heat.For this reason, preferred, before fine coal is carried out to pyrolysis, the less fine powder of the particle diameter in fine coal is removed.
Removal, compared with the fine powder of small particle size, can divide two kinds of modes:
Mode one: carry out sorting by the particle diameter of fine coal, object is for removing the fine particle treat in pyrolyzing coal, avoiding being blended in tar:
As shown in fig. 1, pyrolysis of coal system also comprises fine coal sorting subsystem, for by particle diameter, the fine coal below 0.1mm removes; And transport subsystem (for example, corresponding to the transfer roller 101 in Fig. 1, hopper 71, transfer roller 72 etc.), be suitable for carrying the particle diameter sub-elect from the sorting subsystem fine coal more than 0.1mm to pyrolysis of coal path 10.The sorting of fine coal can be used fluidized-bed to carry out sorting as shown in fig. 1, also can adopt other sorting means.As shown in fig. 1, described sorting subsystem comprises: fluid bed separation path 10 2, fluidizing agent (air or the gases such as flue gas through purifying) is introduced described sort channel 102 and with fluidisation, is arranged in the fine coal of described sort channel from the bottom of described sort channel, the bottom of described sort channel is provided with large particle diameter fine coal relief outlet 103; The second separator 104, the entrance of described the second separator communicates with the top outlet of described sort channel 102, and the pneumatic outlet of described the second separator is discharged fine coal and the fluidizing agent of particle diameter below 0.1mm.Wherein: from described large particle diameter fine coal relief outlet 103, enter described transport subsystem with the fine coal of the solid outlet of described the second separator.In order to remove the moisture in fine coal, in described fluid bed separation path 10 2, be provided with dry heat unit 105, for the fine coal of drying fluidized-bed sort channel, the thermal source of dry heat unit 105 can be from hearth combustion waste heat.As shown in fig. 1, the pneumatic outlet of described the second separator 104 communicates and thinks that burner hearth provides fuel with described burner hearth.So, formed the oily integral process of coal dust sorting (and dry)-burning-pyrolysis-receive.The dry of fine coal for the treatment of pyrolysis can improve pyrolytic tar quality, and efficiency significantly improves.By carrying out pyrolysis by directly sending into pyrolysis of coal passage after the fine coal heating after sorting, can reduce dustiness and water content in coke powder and tar, improve the quality of coke powder and the quality of tar.
It is above-mentioned that by fine coal sorting subsystem, by particle diameter, the fine coal below 0.1mm removes, in actual applications, also can select other particle diameter as the line of delimitation of sorting, such as the particle size range of the fine coal removing is relaxed to 0 ~ 0.5mm or 0 ~ 1mm, or be contracted to the only fine coal of 0 ~ 0.05mm particle size range, depending on the particular cases such as size distribution of the coal of practical application; Adjust the design variable of the second separator 104 and can realize the marginal adjustment of sorting.
Mode two: carry out sorting by the amount of fine coal, the first object is to remove the fine particle treat in pyrolyzing coal, avoid sneaking into tar, the second object is for burner hearth provides appropriate fuel, makes its burning heat release in burner hearth that all heats that provide pyrolysis of coal passage required are provided:
As shown in Figure 4, pyrolysis of coal system also comprises fine coal fluidisation sorting unit, for raw coal is carried out to sorting; And transport subsystem (for example, corresponding to the transfer roller 101 in Fig. 4, hopper 71, transfer roller 72 etc.), be suitable for carrying the larger fine coal of particle diameter sub-electing from sorting subsystem to be transported to pyrolysis of coal path 10.The sorting of fine coal can be used fluidized-bed to carry out sorting as shown in Figure 4, also can adopt other sorting means.As shown in Figure 4, described sorting subsystem comprises: fluid bed separation path 10 2, fluidizing agent (air) is introduced described sort channel 102 and with fluidisation, is arranged in the fine coal of described sort channel from the bottom of described sort channel, the bottom of described sort channel is provided with large particle diameter fine coal relief outlet 103, the top outlet of sort channel communicates with circulating fluidized bed burner hearth 50, the less fine coal of particle diameter (wherein may be entrained with a small amount of large particle diameter fine coal) and fluidizing agent are delivered to burner hearth, as fuel.Wherein, by regulating the fluidized gas scale of construction of sort channel, change the amount of the fine coal that is delivered to burner hearth, the required heat of the burning thermal discharge of this part fine coal in burner hearth and pyrolysis of coal passage is matched, that is:, while not adding other fuel in burner hearth, sort out and add the fine coal of burner hearth should be able to provide pyrolysis of coal passage required net quantity of heat; While also adding other fuel in burner hearth, the combustion heating amount of other fuel can provide pyrolysis of coal passage required heat with the combustion heating amount of the fine coal sorting out.
Between the top outlet of sort channel 102 and circulating fluidized bed burner hearth 50, the tripping device of the second separator 104 in similar Fig. 1 can be set, but also can not establish; And while not establishing tripping device, to fine coal, to be delivered to the adjusting meeting of amount of burner hearth more flexible in sorting; Under carrying effect secretly at elutriation, larger fine coal is also escaped from the top outlet of sort channel, can by the upper design of sort channel, be the settling pocket form that cross-sectional area is larger.In order to remove the moisture in fine coal, in described fluid bed separation path 10 2, can be provided with dry heat unit 105, for the fine coal of drying fluidized-bed sort channel, the thermal source of dry heat unit 105 can be from hearth combustion waste heat.
Fine coal fluidisation sorting unit shown in fine coal sorting subsystem shown in Fig. 1 and Fig. 4, also can be applied in Fig. 2,3 embodiment.
Fig. 5 a is the schematic diagram of the layout between pyrolysis of coal passage according to an embodiment of the invention and solid thermal carriers passage, Fig. 5 b is for representing the height of pyrolysis of coal passage and the exemplary graph of the relation between the temperature of the coal in pyrolysis of coal passage, and Fig. 5 c is for representing the height of pyrolysis of coal passage and the exemplary graph of the relation between gaseous state pyrolysis product amount, relation between the gaseous state pyrolysis product amount that wherein each height location of the exemplary expression pyrolysis of coal of curve I passage and the coal of this At The Height discharge, the height of the exemplary expression pyrolysis of coal of curve II passage and the relation between gaseous state pyrolysis product semi-invariant.
Below the layout between pyrolysis of coal passage and solid thermal carriers passage is specifically described.
As shown in Fig. 5 a, solid thermal carriers A utilizes the fluidizing agent (representing that with arrow R fluid gas passes into figure) passing into from described solid thermal carriers path 10 bottom to flow in described solid thermal carriers path 10 with fluidized state; Coal B adds pyrolysis of coal passage 20 from top, utilize gravity from top to bottom with fluidized state by described pyrolysis of coal passage 20, concurrent raw pyrolytic reaction; Wherein, described pyrolysis of coal passage 20 separate by heat conduction partition 30 with solid thermal carriers path 10 and described solid thermal carriers A and described pyrolysis of coal passage in coal B by described heat conduction partition 30 heat exchange, coal B is heated, occurs pyrolytic reaction.
As shown in Fig. 5 a, described pyrolysis of coal passage 20 comprises from below to up releases most section 21, pyrolysis section 22, heating zone 23, and the coal of releasing most section 21, pyrolysis section 22 and heating zone 23 described in being arranged in is respectively moving-bed state, Micro Fluid state, fluidized state.First the coal being added in pyrolysis of coal passage 20 drops in heating zone 23, by with pyrolysis passage in before add, heated coal short mix is heated, the part volatile matter in coal starts to separate out; Heated coal enters pyrolysis section 22 subsequently, continues heat absorption and pyrolytic reaction fully occurs, and produces a large amount of gaseous state pyrolysis products; Finally, in releasing most section 21, the coal that most of volatile has been disengaged in this section still in comparatively high temps and there is certain residence time, so that volatile matter is separated out as far as possible completely.
Favourable, the solid thermal carriers freeboard of fluidized bed 12 that described solid thermal carriers path 10 correspondingly comprises solid thermal carriers emulsion zone 11 and is positioned at described emulsion zone 11 tops; The position of described pyrolysis section 22 and heating zone 23 is corresponding with the position of described emulsion zone 11.Further favourable, described in release and be arranged in the below of described emulsion zone 11 for most section 21 and do not form heat exchange with the solid thermal carriers A of solid thermal carriers path 10.Coal based on different, the length of releasing most section 21 can be different, so that it releases most volatile matter.
The locational corresponding same length that represents " district " and " section " here, and be positioned at roughly the same level height.It is sign that the change of flow state of material is take in heating zone 23 and the differentiation of pyrolysis section 22, in fact be coal in two sections and absorb in a large number heat, the process of Volatile, therefore generally, section corresponding relation between pyrolysis of coal passage 20 and solid thermal carriers path 10, need satisfied condition be: the fluidized-bed bed surface 24(that the coal of pyrolysis of coal passage forms is the fluidized-bed bed surface of heating zone 23) can not be significantly lower than the bed surface of solid thermal carriers emulsion zone 11, otherwise will there is second pyrolysis in the gaseous state pyrolysis product that continues to make progress mobile from fluidized-bed bed surface 24 under the violent heat effect of solid thermal carriers emulsion zone 11, affect the quality of tar.Therefore, the position of described pyrolysis section 22 is roughly corresponding with the position of described emulsion zone, and the position of described heating zone 23 is roughly corresponding with the position of described freeboard of fluidized bed 12, is also one of optional scheme.
Coal adds from the top of pyrolysis of coal passage 20, enters successively heating zone 23, pyrolysis section 22, releases most section 21.Size that can appropriate design pyrolysis section, makes to maintain fluidized state in pyrolysis of coal process, reaches best effect.Coal, in the process moving down, is constantly heated, and moisture and volatile matter are separated out in a large number, while arriving pyrolysis section bottom, separates out substantially completely, enters and releases the most section of coal by pyrolysis (semicoke) and become moving-bed, favourable, can after cooling, discharge.Or, without cooling direct discharge, this is particularly applicable for oil shale pyrolysis, because remaining shale semicockes calorific value is lower after oil shale pyrolysis, unlike remaining semicoke after pyrolysis of coal, can also supply outward as product, shale semicockes without cooling, be directly delivered to hearth combustion, both can realize stable burning, can make full use of again this difficult low heat value product utilizing.
The residence time of coal in pyrolysis of coal passage 20 separated out required asynchronism(-nization) and different according to fugitive constituent, and this can be by substantially judging by temperature survey in pyrolytic process.Can adjust the output of load and the bottom semicoke of pyrolysis passage, make pyrolysis section corresponding with the emulsion zone of solid thermal carriers with heating zone.The freeboard of fluidized bed granule density on emulsion zone top is low, and heat transfer effect weakens, excess Temperature while just in time avoiding tar in gaseous state pyrolysis product to discharge from pyrolysis of coal passage top and second pyrolysis occurs.
In Fig. 5 b, heating zone 23 corresponding to temperature from 200 ℃ be rapidly heated to 600 ℃ of left and right section, pyrolysis section 22 corresponding to temperature be roughly stabilized in 600 ℃ of left and right section, and release corresponding to temperature, 600 ℃ of left and right, slightly decline for most section 21 section.At coal, from pyrolysis of coal passage top, add, fall into the process of heating zone, the coal that adds is preheated, temperature slightly rises, and discharges a small amount of gaseous state pyrolysis product.Gaseous state pyrolysis product mainly disengages from pyrolysis section 22.The temperature range is here only schematically, and for different coals, this temperature may be different.
As shown in Figure 5 c, in releasing most section, the gaseous state pyrolysis product of generation seldom, the gaseous state pyrolysis product that accumulation produces also seldom, thereby the semicoke moving-bed state in non-fluidisation substantially.And in pyrolysis section, a large amount of gaseous state pyrolysis products are precipitated, thereby the coal in pyrolysis section can be in Micro Fluid state (understandable, low in the fluidisation degree of the coal on pyrolysis section top in the fluidisation degree of the coal of pyrolysis section bottom).Owing to all making progress and flow from releasing gaseous state pyrolysis product that most section, pyrolysis section disengage, and add up mutually with the gaseous state pyrolysis product that coal discharges in heating zone, therefore the coal in heating zone is substantially all in fluidized state.
In the situation that the gaseous state pyrolysis product of pyrolysis of coal passage 20 interior generations is enough to maintain the fluidized state of Micro Fluid state and the coal in heating zone of the coal in pyrolysis section, do not need to pass into other fluidizing agent, that is the gaseous state pyrolysis product that, coal B utilizes the 20 interior generations of pyrolysis of coal passage with the state of self-fluidized type by described pyrolysis of coal passage 20.
In the situation that the gaseous state pyrolysis product of pyrolysis of coal passage 20 interior generations is not enough to maintain the fluidized state of Micro Fluid state and the coal in heating zone of the coal in pyrolysis section, can pass in the bottom of pyrolysis of coal passage other fluidizing agent, that is: coal B utilize the gaseous state pyrolysis product of pyrolysis of coal passage 20 interior generations and the other fluidizing agent that passes into from pyrolysis of coal passage 20 bottoms with the state of fluidisation by described pyrolysis of coal passage 20.Favourable, described other fluidizing agent is pyrolysis gas, hydrogen, methane or other non-oxidizing gas.
Although comprise heating zone, pyrolysis section at pyrolysis of coal passage shown in Fig. 5 a, release most section,, in the sufficient situation of pyrolysis, also can save this and release most section.
Favourable, described coal generation pyrolytic reaction, the gaseous product of generation is discharged from described pyrolysis of coal channel roof.But, the gaseous product of generation also can be discharged the side from pyrolysis of coal passage top partly.
Favourable, enter the particle diameter of coal of described pyrolysis of coal passage between 0.1mm-12mm.Select such particle size range to have following advantage: to contribute to the fluidization of coal particle; Contribute to the pyrolysis of coal; Contribute to reduce the dustiness in pyrolysis oil gas.
Further describe the decoration form of heat exchanger for pyrolysis of coal below.
As shown in Fig. 5 a, described solid thermal carriers path 10 arranges around described pyrolysis of coal passage 20.
As shown in Figure 6, described pyrolysis of coal passage 20 is for being arranged in many thermal decomposition tubes 20 ' in described solid thermal carriers path 10.The upper end of these many thermal decomposition tubes 20 ' can also communicate with common feeding-passage, and the lower end of these many thermal decomposition tubes 20 ' also can communicate with common tapping channel.
Referring to Fig. 7-8, the quantity of described solid thermal carriers path 10 and described pyrolysis of coal passage 20 is all at least one; And described solid thermal carriers path 10 and described pyrolysis of coal passage 20 be almost parallel and being alternately arranged with each other each other, the space that the space between adjacent solid thermal carriers path 10 forms between a pyrolysis of coal passage 20 and/or adjacent pyrolysis of coal passage 20 forms a solid thermal carriers path 10.In Fig. 7, solid thermal carriers path 10 and pyrolysis of coal passage 20 form the form of " sandwich biscuit ".In Fig. 8, solid thermal carriers path 10 and pyrolysis of coal passage 20 form the form of a plurality of " concentric drums ".
Although do not illustrate, can, by design heat conduction partition 30, such as making it have blossom type cross section, heat conduction fin etc. being set on heat conduction partition, make the heating surface area of heat conduction partition 30 increase to strengthen heat transfer effect.
In the situation that described solid thermal carriers cycling stream is crossed described solid thermal carriers passage, as shown in Figure 9, the sidewall of described solid thermal carriers passage is provided with overflow port 15, thereby from solid thermal carriers path 10, discharges solid thermal carriers to keep stable emulsion zone height in the mode of overflow.In addition, the relief outlet of solid thermal carriers also can be located at the bottom of solid thermal carriers path 10, now needs material level to monitor, to keep stable emulsion zone height.In Fig. 9, solid thermal carriers A introduces from the opening 16 of the bottom of solid thermal carriers path 10, but, solid thermal carriers A also can introduce (as shown in Fig. 1-4) from the top of solid thermal carriers path 10, in addition, the mode of introducing is not limited to opening, also can use pipeline directly to pass into.
Stable emulsion zone height contributes to the coal in pyrolysis section to receive stable heat and by stable pyrolysis.
The following describes according to pyrolysis of coal method of the present invention.
Pyrolysis of coal method according to an embodiment of the invention can comprise the steps: to pass into fluidizing agent (as shown in arrow R in Fig. 5 a) in solid thermal carriers path 10 bottom, and solid thermal carriers A is flowed in solid thermal carriers path 10 with fluidized state, to utilizing heat conduction partition 30 and the interior feeding pulverized coal B of the separated pyrolysis of coal passage 20 of solid thermal carriers path 10, wherein, described fine coal B utilize gravity from top to bottom with fluidized state by described pyrolysis of coal passage 20, coal B in described solid thermal carriers A and described pyrolysis of coal passage is by 30 heat exchange of heat conduction partition, coal is heated, there is pyrolytic reaction, wherein: described solid thermal carriers path 10 is arranged in the circulation loop of circulating fluidized bed burner hearth outside, the solid thermal carriers entrance of described solid thermal carriers path 10 with and the solid outlet of the separator 60 that is communicated with of furnace outlet flue communicate, the sidewall of described solid thermal carriers passage is provided with overflow port 15, described overflow port 15 communicates with the returning charge mouth 51 of burner hearth 50.
Favourable, described pyrolysis of coal method also comprises step: in burner hearth or solid thermal carriers path 10, add the inert particle as solid thermal carriers.Favourable, described solid thermal carriers comprise fuel pellet and solid-state products of combustion thereof.
Pyrolysis of coal method above all can comprise the steps: to provide fine coal, and the fine coal below 0.1mm removes by particle diameter to utilize a minute selection operation; And to supplying with the particle diameter that the sub-elects fine coal more than 0.1mm in pyrolysis of coal passage.Favourable, described pyrolysis of coal method also comprises step: the fine coal by particle diameter below 0.1mm is sent to stove chamber inner combustion.Or comprise the steps: to provide fine coal, and utilize a minute selection operation that fine coal is divided into two portions, the larger part fine coal of particle diameter of discharging from the lower part outlet of sorting unit is delivered to pyrolysis of coal passage, and the less part fine coal of particle diameter of discharging from the outlet of sorting unit top is delivered to hearth combustion.Wherein, by adjusting, pass into the fluidized gas scale of construction of sorting unit, regulate the coal amount that is transported to burner hearth from the outlet of sorting unit top, the required heat of its combustion heating amount and pyrolysis of coal passage is matched.
Although illustrated and described embodiments of the invention, for the ordinary skill in the art, be appreciated that without departing from the principles and spirit of the present invention and can change these embodiment.The scope of application of the present invention is limited by claims and equivalent thereof.
Claims (34)
1. for a pyrolysis system for solid carbon material, comprising:
Circulating fluidized bed burner hearth;
The first separator being connected with the exhanst gas outlet of circulating fluidized bed;
Solid thermal carriers passage, solid thermal carriers flow in described solid thermal carriers passage with fluidized state;
Pyrolysis passage, particulate state adds from top containing the solid carbon material of volatile matter, utilize gravity from top to bottom with fluidized state by described pyrolysis passage, concurrent raw pyrolytic reaction,
Wherein:
Described pyrolysis passage and solid thermal carriers passage by heat conduction partition, separate and described solid thermal carriers and described pyrolysis passage in solid carbon material by the heat exchange of described heat conduction partition, solid carbon material is heated, occurs pyrolytic reaction;
The solid thermal carriers entrance of described solid thermal carriers passage communicates with the solid outlet of described the first separator, and the sidewall of described solid thermal carriers passage is provided with overflow port, and described overflow port communicates with the returning charge mouth of burner hearth.
2. the pyrolysis system for solid carbon material according to claim 1, wherein:
Described pyrolysis passage comprises many thermal decomposition tubes or a plurality of pyrolysis passage being arranged in described solid thermal carriers passage.
3. the pyrolysis system for solid carbon material according to claim 1, wherein:
Described solid thermal carriers comprise the inert particle joining in burner hearth or solid thermal carriers passage.
4. the pyrolysis system for solid carbon material according to claim 3, wherein:
At least a portion pyrolysis product from the outlet of described pyrolysis passage top is fed into burner hearth as fuel.
5. the pyrolysis system for solid carbon material according to claim 4, wherein:
Described at least a portion pyrolysis product comprises heavy tar and/or pyrolysis gas.
6. the pyrolysis system for solid carbon material according to claim 3, wherein:
The particle size range of described inert particle is 0-2mm.
7. the pyrolysis system for solid carbon material according to claim 3, wherein:
In described solid thermal carriers passage, add the fuel that is useful on heat solid thermal barrier.
8. the pyrolysis system for solid carbon material according to claim 1, wherein:
Described solid carbon material is coal, resinous shale, dewatered sludge or biological particles.
9. the pyrolysis system for solid carbon material according to claim 8, wherein:
The particle diameter of described solid carbon material is within the scope of 0-12mm.
10. the pyrolysis system for solid carbon material according to claim 9, also comprises:
Sorting subsystem, the solid carbon material by particle diameter below 0.1mm removes; And
Transport subsystem, is suitable for carrying the particle diameter sub-elect from the sorting subsystem solid carbon material more than 0.1mm to pyrolysis passage.
11. pyrolysis systems for solid carbon material according to claim 10, wherein:
Described sorting subsystem comprises:
Fluid bed separation passage, fluidizing agent is introduced described sort channel and with fluidisation, is arranged in the solid carbon material of described sort channel from the bottom of described sort channel, and the bottom of described sort channel is provided with large particle diameter solid carbon material relief outlet;
The second separator, the entrance of described the second separator communicates with the outlet of the top of described sort channel, and the pneumatic outlet of described the second separator is discharged solid carbon material and the fluidizing agent of particle diameter below 0.1mm,
Wherein: from described large particle diameter solid carbon material relief outlet with from the solid carbon material of the solid outlet of described the second separator, enter described transport subsystem.
12. pyrolysis systems for solid carbon material according to claim 11, wherein:
In described fluid bed separation passage, be provided with dry heat unit, for the solid carbon material of drying fluidized-bed sort channel.
13. pyrolysis systems for solid carbon material according to claim 11, wherein:
The pneumatic outlet of described the second separator communicates and thinks that burner hearth provides fuel with described burner hearth.
14. pyrolysis systems for solid carbon material according to claim 1, wherein:
Described solid carbon material pyrolysis system also comprises solid carbon goods fluid sorting unit, the solid carbon material of discharging from the top outlet of sorting unit is transported to circulating fluidized bed burner hearth, and the solid carbon material of discharging from the lower part outlet of sorting unit is transported to described pyrolysis passage.
15. pyrolysis systems for solid carbon material according to claim 14, wherein:
The described solid carbon material of discharging, be transported to burner hearth from the outlet of sorting unit top, the required heat of its combustion heating amount and pyrolysis passage matches.
16. pyrolysis systems for solid carbon material according to claim 1, wherein:
The solid thermal carriers freeboard of fluidized bed that described solid thermal carriers passage comprises solid thermal carriers emulsion zone and is positioned at described emulsion zone top;
Solid carbon material in described pyrolysis passage has at least a part to be fluidized-bed state, and forms fluidized-bed bed surface,
Wherein, the bed surface of described solid thermal carriers emulsion zone substantially with described pyrolysis passage in fluidized-bed bed surface contour, or a little less than the latter.
17. pyrolysis systems for solid carbon material according to claim 16, wherein:
Described pyrolysis passage comprises pyrolysis section, heating zone from bottom to top, and the solid carbon material that is arranged in described pyrolysis section and heating zone is respectively Micro Fluid state and fluidized state.
18. pyrolysis systems for solid carbon material according to claim 17, wherein:
The position of described pyrolysis section and heating zone is roughly corresponding with the position of described emulsion zone.
19. pyrolysis systems for solid carbon material according to claim 17, wherein:
The position of described pyrolysis section is roughly corresponding with the position of described emulsion zone, and the position of described heating zone is roughly corresponding with the position of described freeboard of fluidized bed.
20. pyrolysis systems for solid carbon material according to claim 16, wherein:
Described pyrolysis passage comprises from below to up releases most section, pyrolysis section, heating zone, and the solid carbon material of releasing most section, pyrolysis section and heating zone described in being arranged in is respectively moving-bed state, Micro Fluid state, fluidized state.
21. pyrolysis systems for solid carbon material according to claim 20, wherein:
The position of described pyrolysis section and heating zone is roughly corresponding with the position of described emulsion zone.
22. pyrolysis systems for solid carbon material according to claim 21, wherein:
The position of described pyrolysis section is roughly corresponding with the position of described emulsion zone, and the position of described heating zone is roughly corresponding with the position of described freeboard of fluidized bed.
23. pyrolysis systems for solid carbon material according to claim 21, wherein:
Describedly release most section of below that is arranged in described emulsion zone and do not form heat exchange with the solid thermal carriers of solid thermal carriers passage.
24. pyrolysis systems for solid carbon material according to claim 1, wherein:
Described solid carbon material utilize the gaseous state pyrolysis product that produces in pyrolysis passage with the state of self-fluidized type by described pyrolysis passage.
25. pyrolysis systems for solid carbon material according to claim 1, wherein:
Described solid carbon material utilize the gaseous state pyrolysis product producing in pyrolysis passage and the other fluidizing agent passing into from pyrolysis passage bottom with the state of fluidisation by described pyrolysis passage.
26. pyrolysis systems for solid carbon material according to claim 25, wherein:
Described other fluidizing agent is pyrolysis gas, hydrogen, methane or other non-oxidizing gas.
27. pyrolysis systems for solid carbon material according to claim 1, also comprise:
Refrigerating unit, the solid product that discharge from pyrolysis passage after for the pyrolysis of cooling solid carbonaceous material the below that described refrigerating unit is arranged in described pyrolysis passage.
The method for pyrolysis of 28. 1 kinds of solid carbon materials, comprises step:
In solid thermal carriers channel bottom, pass into fluidizing agent, solid thermal carriers are flowed in solid thermal carriers passage with fluidized state;
To utilizing in the separated pyrolysis passage of heat conduction partition and solid thermal carriers passage, supply with particulate state containing the solid carbon material of volatile matter, wherein, described solid carbon material utilize gravity from top to bottom with fluidized state by described pyrolysis passage, solid carbon material in described solid thermal carriers and described pyrolysis passage is by the heat exchange of heat conduction partition, make solid carbon material be heated, occur pyrolytic reaction
Wherein: described solid thermal carriers channel setting is in the circulation loop of circulating fluidized bed burner hearth outside, the solid thermal carriers entrance of described solid thermal carriers passage with and the solid outlet of the separator that is communicated with of burner hearth flue communicate, the sidewall of described solid thermal carriers passage is provided with overflow port, and described overflow port communicates with the returning charge mouth of burner hearth.
The method for pyrolysis of 29. solid carbon materials according to claim 28, wherein:
Described solid thermal carriers comprise fuel pellet and solid-state products of combustion thereof.
30. method for pyrolysis containing solid carbon material according to claim 29, also comprise step:
In burner hearth or solid thermal carriers passage, add the inert particle as solid thermal carriers.
31. according to the method for pyrolysis of the solid carbon material described in any one in claim 28-30, also comprises step:
The solid carbon material that provides particulate state to contain volatile matter, and the solid carbon material below 0.1mm removes by particle diameter to utilize a minute selection operation; And
To supplying with the particle diameter that the sub-elects solid carbon material more than 0.1mm in pyrolysis passage.
The method for pyrolysis of 32. solid carbon materials according to claim 31, also comprises step:
Solid carbon material by particle diameter below 0.1mm is sent to stove chamber inner combustion.
33. according to the method for pyrolysis of the solid carbon material described in any one in claim 28-30, also comprises step:
Solid carbon mass transport is arrived to solid carbon goods fluid sorting unit, the solid carbon material of discharging from the top outlet of sorting unit is transported to circulating fluidized bed burner hearth, and the solid carbon material of discharging from the lower part outlet of sorting unit is transported to described pyrolysis passage.
The method for pyrolysis of 34. solid carbon materials according to claim 33, wherein:
Adjusting passes into the fluidized gas scale of construction of sorting unit, so that be transported to the combustion heating amount of the solid carbon material of burner hearth from sorting unit, the heat required with pyrolysis passage matches.
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