CN108018053A

CN108018053A - Genealogical classification coke discharging method and apparatus is burnt in the hydrocarbon powder pyrolysis of solid heat carrier method

Info

Publication number: CN108018053A
Application number: CN201610950444.0A
Authority: CN
Inventors: 何巨堂
Original assignee: 何巨堂
Current assignee: Luoyang Rui Hua new energy technology development Co., Ltd.
Priority date: 2016-10-28
Filing date: 2016-10-28
Publication date: 2018-05-11

Abstract

Genealogical classification coke discharging method and apparatus is burnt in the hydrocarbon powder pyrolysis of solid heat carrier method, it is suitable for pulverized coal pyrolysis fluid bed burning process, in system UNIT is burnt using the hydrocarbon powder R10FS of solid thermal carriers R10KS pyrolysis, solid thermal carriers R10KS circulate by arbitrary procedure position, isolate at least a portion little particle LS under the critical grain size DZ in the material EM comprising solid thermal carriers and collect, discharge recycling, to reduce the concentration of solid thermal carriers small particles LS, the dedirt load of pyrolytic reaction gas-solid product can be significantly reduced, reduce solids content in pyrolytic tar.

Description

Genealogical classification coke discharging method and apparatus is burnt in the hydrocarbon powder pyrolysis of solid heat carrier method

Technical field

The present invention relates to the hydrocarbon powder pyrolysis of solid heat carrier method to burn genealogical classification coke discharging method and apparatus, is suitable for powder Pyrolysis of coal fluid bed burning process, in system UNIT is burnt using the hydrocarbon powder R10FS of solid thermal carriers R10KS pyrolysis, Solid thermal carriers R10KS circulate by arbitrary procedure position, isolate in the material EM comprising solid thermal carriers At least a portion little particle LS under critical grain size DZ is simultaneously collected, is discharged recycling, to reduce solid thermal carriers small particles The concentration of LS, can significantly reduce the dedirt load of pyrolytic reaction gas-solid product, reduce solids content in pyrolytic tar.

Background technology

Hydrocarbon powder of the present invention, refers to that in pyrolytic reaction process of the present invention containing containing oil vapour can be produced There is a powder of carbon, protium, such as the high low-disintegration coal powder of volatile matter content, oil-sand, oil shale, DCL/Direct coal liquefaction generation Oily vacuum fractionation tower bottom of towe contains and contains oil residue admittedly.

Large coal mine such as low-disintegration coal ore deposit generally use mechanization fully mechanized mining technology is modernized to improve coal mining efficiency, reduce Cost, the fine coal yield in its coal extraction product is about 60~70%, becomes main product, therefore the deep conversion of fine coal and comprehensive The principal status of public economy that will be occupied modern low-disintegration coal charcoal using technology and utilize technology is closed, a branch field of fine coal processing is " fine coal sub-prime classified utilization ", wherein pulverized coal pyrolysis is considered as the technological approaches for having economic competitiveness.

Fine coal FM, that is, R10FS of the present invention, fine coal is dehydrated after usually drying, its moisture weight is usually less than 10%, Generally below 7%, preferably is less than 5%.

Fine coal FM, that is, R10FS of the present invention, its granularity are usually 0.00001~6 millimeter, are generally 0.0001~3.5 Millimeter, preferably are 0.001~2 millimeter.

Pulverized coal pyrolysis process of the present invention, refers to that using voluminous coal tar be process goal in suitable temperature range The pulverized coal pyrolysis process of interior operation, can be any one suitable form.

The major product of pulverized coal pyrolysis process is tar, coal gas, semicoke, wherein tar be considered as potential age deduction most Big product, it is usually desirable to improve its yield and/or hydrogen content.

The main target of pulverized coal pyrolysis commercial technologies is：Raising fine coal high value component recovery rate (or improve fine coal height Value product yield), improve list covering device processing capacity, the reliability and controllability that reduce specific energy consumption, develop skill；Therefore, Notable breakthrough only is obtained in said one or several targets, the economy of industrial technology could be supported, and eventually becomes master The pulverized coal pyrolysis commercial technologies of stream.

So far, multiple industrial states or large scale business company research and develop pulverized coal pyrolysis technology, have carried Go out kinds of processes such as the Germany i.e. Lu Qi of L-R techniques-Rule technique, U.S.'s Toscoal techniques, U.S.'s COED techniques, but there is no The successful case that large scale business makeup is put.

Above-mentioned typical case's pulverized coal pyrolysis technology, says from engineering technology angle, can not comprehensively or substantially eliminate following defects, root It is that rationally fusion does not integrate by the technological means for realizing different target：

1. the Thermodynamic Mechanism of pyrolytic reaction is unintelligible, the body operation temperature of single pyrolytic reaction process is positioned beyond 500 DEG C of narrow temperature, does not possess classification pyrolysis function, can not take into account the difference of the pyrolytic reaction in fine coal different temperatures stage Different, the parallel reaction of shortage pyrolysis of coal process, the selective control ability of the reaction depth of cascade reaction, cause tar yield It is low, hydrogen content is low；

2. the heat-supplying mode of pyrolytic reaction industrial process is unreasonable, hydrodynamic characteristic is unreasonable and device structure does not conform to Reason, causes too short i.e. poor reliability service cycle, is not easy to realize maximization, causes throughput per unit investment big；

3. heat reclaiming system integrated level is too low, cause system thermal efficiency low；

4. pyrolysis step integrated level is too low, operating procedure is more, system complex poor reliability.

In general, the different pyrolytic reactions of the high coal of volatile matter content are present in the wider pyrolysis temperature such as 380~680 DEG C In the range of degree, for reaction type, pulverized coal pyrolysis process will point to different mesh there are numerous parallel reaction and cascade reaction For the approach direction for marking product, mainly there is the Pyrolysis of the macromolecular generation smaller molecular weight product (coal gas and tar) of coal Answer 2 or multiple centres of (the secondary heat scission reaction for including a heat scission reaction, thermal cracking products) and pyrolysis of coal process The condensation of product free radical is the condensation reaction of macromolecule product, therefore, in order to improve tar yield, improve tar hydrogen content, On the one hand need increase to produce the heat scission reaction of the coal of tar, on the one hand need to suppress the consecutive condensation of tar product.

The multistage method for pyrolysis that COED techniques use, the classification pyrolysis of heating step by step that classification pyrolytic reaction condition meets coal will Ask, the yield of pyrolytic tar can reach 18~22% and best in quality, and still, operating procedure that this method includes is too many, system Complicated, poor reliability；In addition dry distillation of coal process heat-supplying mode only used gas heat carrier without using solid thermal carriers, its Heat carrier unit volume, the thermal capacity of unit mass are smaller, and heat transfer rate is relatively low, and reaction compartment volume is necessarily huge, is unfavorable for Maximization.

With the appearance of CN105602593A, CN105694933A method, the above situation is changed substantially, its basic principle It can be regarded as petroleum industry wax oil or the reaction-regeneration system skill in the fluidized catalytic cracking field of residual oil to a certain extent The graft application of art.In the fluidized catalytic cracking reaction-regeneration system of residual oil, raw material that one way passes through be atomization residual oil, Its product is gaseous breakdown oil gas, and the material of cyclic process is powdery solid catalyst, discharges riser catalytic thermal cracking reaction The catalyst of device is coking rear catalyst solid, and cyclone separation system of the coking rear catalyst by arrangement in settler is completed de- Gas, subsequently into making charcoal, device or regenerator carry out coke-burning regeneration, and the regenerated catalyst powder of high temperature state is as solid thermal carriers The lower entrances of riser reactor are returned with catalyst, under lift gas effect, progress is mixed with the residual oil of atomization Fluidized catalytic cracking reaction, at least a portion heat that regenerator produces are returned riser catalytic thermal cracker again Hot catalyst is loaded into the heat source that riser catalytic thermal cracker serves as thermal cracking process after life.Residual oil fluidized catalytic is split The reaction-regeneration system of change, has had more than the successful operating history of 50 years, its monosystem array apparatus process residual oils amount that maximizes is reachable 400~8,000,000 tons/year, catalyst circulation amount up to 2000~40,000,000 tons/year i.e. 2500~5000 tons/when.

Compared with the fluidized catalytic cracking reaction-regeneration system of wax oil or residual oil, CN105602593A, CN105694933A methods, carry out pulverized coal pyrolysis reaction, using similar cyclonic separation system using similar riser reactor The gas solid separation for (being arranged in settler) completion pulverized coal pyrolysis reaction product of uniting, coke breeze oxygen deprivation is carried out using similar device of making charcoal Burning, a part for the hot semicoke that device of making charcoal produces enter riser reactor to pyrolysis of coal reaction process as solid thermal carriers Heat supply simultaneously forms the circulatory system, unnecessary semicoke discharge system and/or oxidizing fire release heat.CN105602593A, In system described in CN105694933A, the raw material that one way passes through is fresh solid fine coal, its pyrolysis product is gaseous state coal gas and consolidates Body semicoke, the material of cyclic process is solid semicoke (semicoke product of pyrolytic reaction or semicoke cycle stock), and high temperature state is consolidated Body aoxidizes the lower entrances that semicoke returns to riser reactor as solid thermal carriers, under lift gas effect, with fresh coal Powder, which is mixed, carries out fluidization pyrolytic reaction.

It can be seen that pyrolysis reactor, thermal decomposition product gas solid separation system, the pyrolysis solid of two kinds of technologies from above-mentioned contrast Product settler, solid circle material are made charcoal device, and the type of flow of the gas-solid fluid of its identical workflow position is essentially identical.Due to two The above-mentioned similitude of person, CN105602593A, CN105694933A method, greatly simplifie system structurally and operationally, pole The earth improves the security of system, is the technical method of deep tool large industrialized potentiality, has the advantage that：

1. the Thermodynamic Mechanism of pyrolytic reaction is clear, using self-heating solid thermal carriers, the table with lifting air lift for powder Face energy and uplink kinetic energy, potential energy, realize the discretization of solid powder and quickly gather and divide, enhance heat transfer rate, realize fast Speed heat solution；

2. rationally (system self-heating, fuel are low value semicoke), hydrodynamics are special for the heat-supplying mode of pyrolytic reaction process Property rationally (riser provides solid material level energy, settler utilizes gravity acting downlink) and device structure it is reasonable, reliability height is Service cycle is grown, it is easy to accomplish maximization, can reduce throughput per unit investment；

3. heat reclaiming system is highly integrated, system thermal efficiency is high；

4. pyrolysis, applying heat are highly integrated, operating procedure is few, and simple system, reliability are high.

However, " the powder formed using the pulverized coal pyrolysis process of oxidation semicoke solid thermal carriers with pyrolysis char burning process Pyrolysis of coal and burn system CTC-UNIT ", the fluidized catalytic cracking reaction-regeneration system with wax oil or residual oil comparatively, In terms of the grain diameter tendency of changes and border restriction scheme of solid circle heat carrier, there is entirely different mechanism, main table It is now：

1. in general, the particle size range for the powdery catalytic cracking catalyst that modern catalytic cracking reaction process uses is relatively narrow, than If any it is a small amount of be less than 10 microns of particles for being even less than 1 micron, have a large amount of 20~180 microns of particle, also have it is minimal amount of big In 180 microns of particle；The regenerated catalyst of wait of reclaimable catalyst, that is, settler discharge is flammable focus layer shell and not The particle of molecular " the focus layer bag stone " double-decker of flammable catalyst pellets, because (surfaces externally and internally) is burnt on coked catalyst Carbon content relatively low (usually less than 15%, generally below 10%), catalyst are incombustible inert substance in itself, solid particle Interior incendivity reactant is less, and in reaction process is burnt, the change of size of solids is little, and such regenerated catalyst is (i.e. Coke burning regeneration rear catalyst) particle diameter and reclaimable catalyst particle diameter, can usually regard as roughly it is equal, also It is to say, the particle diameter of reclaimable catalyst is to the particle diameter of regenerated catalyst " naturally with grain diameter tendency of changes Lower boundary limit acts on "；Certainly, other processes such as cyclone separator in riser reactor, settler, settler, burn The flowing containing solid material in cyclone separator, solid material conveying pipe road and valve in device because particle and particle it Between collision, the collision of particle and channel wall, effect, the crushing mechanism such as burst apart can cause a small amount of major diameter particle to minor diameter The change of particle；

2. and the particle size range of the solid semicoke dust in pulverized coal pyrolysis product CCP is wider, has and be largely less than 10 microns very (come from raw material fine coal, the collision crashing from flow process, from fluid bed burning process to the particle less than 1 micron Burn the little particle that undergauge produces), have a large amount of 20~180 microns of particle, also have a large amount of 180~2000 microns even 2000~ 6000 microns of particle；Certainly, other processes such as cyclone separator in riser reactor, settler, settler, burn device The flowing containing solid material in interior cyclone separator, solid material conveying pipe road and valve, because between particle and particle Collision, the collision of particle and channel wall, effect, the crushing mechanism such as burst apart can cause major diameter particle to small diameter particles Change；And the diffusion impact to outside particle of the splitting of pulverized coal pyrolysis gas making, gas, fine coal intensity are usually less than catalytic cracking and urge The collective effect of these factors of agent intensity so that fine coal, semicoke are easier fragmentation compared with catalytic cracking catalyst and produce more, grain The crushed material of footpath smaller, that is, fine coal little particle, semicoke little particle；

But, it is even more important that the pyrolysis char of settler discharge is the particle of Whole Flammable (when particle is without inorganic During thing kernel) or the almost particle (when particle kernel containing organic/inorganic substance) of Whole Flammable, incendivity reactant in solid particle Close to 100%, in reaction process is burnt, the particle diameter of solids progressively diminishes until last disappear (when particle is without inorganic During thing kernel), or the particle diameter of solids progressively diminishes until eventually form fine ash (when particle kernel containing inorganic matter), this The particle diameter of the oxidation semicoke of sample semicoke burning process is exactly the dynamic value in the range of one 0 to reclaimable catalyst particle diameter DIN, That is the particle diameter " naturally with grain diameter tendency of changes in zero tendency " of semicoke, of pyrolysis char are aoxidized Particle diameter " naturally border restriction effect without grain diameter tendency of changes " of the grain diameter to oxidation semicoke.

In fluid bed burning process, Air for burning coke, that is, fluidized wind forms flotation effect to burning semicoke particle in reactor, In this way, the small particle semicoke that unit mass external surface area is big, buoyancy/particle weight ratio is big, has in fluid bed burning process Following features：

1. small particle semicoke, short in the dense bed residence time than big particle diameter semicoke；

2. dilute-phase leanphase fluidized bed semicoke particle is mainly small particle semicoke, the small particle semicoke weight concentration on dense bed top is higher than close The small particle semicoke weight concentration of phase bed lower part, i.e. dense bed top are enriched with small particle semicoke；

3. the oxygen concentration in burn wind or flue gas, along dense bed lower part → dense bed top → dilute-phase leanphase fluidized bed lower part → dilute phase Bed top gradually reduces, and the distribution of this oxygen concentration, is unfavorable for the burning of small particle semicoke；

4. on " dense bed top → dilute-phase leanphase fluidized bed lower part → dilute-phase leanphase fluidized bed top → flue gas cyclone separator → flue gas cyclonic separation The small particle semicoke circulation loop that device semicoke decline dipleg " is formed, there is the tendency that circulation accumulation forms huge internal circulating load.

Above-mentioned analysis implies, in the burning process of pyrolysis char, " needs human intervention, can just make oxidation semicoke product Grain diameter change to be formed border limitation ", in other words to ensure in other words according to the pre- of solid thermal carriers grain diameter Phase is distributed, and can carry out classification coke discharging to burning semicoke grain graininess in reactor as needed, so that rationally control is used as admittedly The particle size distribution of the oxidation semicoke product of body heat carrier, its process goal and technological effect are：

1. selectivity reduces the reserve of the particle of semicoke burning process small particle scope, amount of burnt

When needing bulky grain solid heat carrier and little particle semicoke product, to burning semicoke particle in reactor, utilize The flotation function of fluidized wind, forms big grain particles bed and small size particle bed (or accumulation regions), big grain particles bed is using most Good fluidization conditions carry out burning the optimal scorching speed that reaction or control need, and big grain particles bed discharge material, which is formed, to be needed The solid thermal carriers of particle diameter, can also form the bulky grain solid semicoke product of needs；And small size particle bed (or accumulation regions) Semicoke then can individually be discharged as little particle semicoke product, such as during preferential discharge little particle semicoke, although little particle semicoke It is low but its reserve can be reduced to burn rate, the circulation for burning that flue gas gas solid separation system is isolated in reactor can be significantly reduced Flow back semicoke mass flow, substantially reduces and burns amount of burnt in reactor；

2. formation preferably burns operating condition

When needing to use solid small particles heat carrier and bulky grain semicoke product, the flotation function of fluidized wind, shape are utilized Into big grain particles bed and small size particle bed (or accumulation regions), small size particle bed is burnt using optimal fluidization conditions The optimal scorching speed that reaction or control need, small size particle bed are discharged the solid thermal carriers to form needs, can also be formed The solid small particles semicoke product needed；And the semicoke of big grain particles bed (or accumulation regions) then can preferentially be discharged and burnt with reducing Jiao Liang；The circulating reflux semicoke mass flow that flue gas gas solid separation system in reactor of burning is isolated can be significantly reduced；Can Amount of burnt in reactor is burnt to reduce；

The little particle of quantity is needed to aoxidize half 3. discharge needs the bulky grain of quantity to aoxidize semicoke solid thermal carriers and discharge Burnt solid thermal carriers, flexibly control the size distribution of mixed oxidization semicoke solid thermal carriers；

The little particle oxidation semicoke of quantity is needed to consolidate 4. discharge needs the bulky grain of quantity to aoxidize semicoke product and/or discharge The size distribution of body product, flexibly control oxidation semicoke solid product；

5. using bulky grain oxidation semicoke solid thermal carriers, little particle semicoke quantity in pyrolytic reaction product can be reduced, The gas for reducing pyrolytic reaction product takes off solid load, reduces the solid semicoke content in tar liquid product；

6. reaction process can burnt, semicoke particle aggregation area and the exhaust system of multiple and different particle diameters are formed, so that The semicoke of a variety of different-grain diameters can be obtained, by way of classifying and using or be used in mixed way, obtains the half of a variety of different-grain diameters Burnt solid thermal carriers and/or semicoke product.

The semicoke whereabouts for usually burning system is broadly divided into 5：

1. balancing amount of burnt, the thermal energy of generation brings riser pulverized coal pyrolysis reactor into by solid thermal carriers oxidation semicoke In；

2. thermal energy changes amount of burnt, for the material of neighbouring unit or device thermal energy is provided water vapour, heating gas such as occurs；

3. hot half coke fuel discharged；

For example it is directly entered fluidized bed boiler systems and realizes that heat integration produces cogenerated products；

Stored after the hot semicoke product of discharge, such as recycling thermal energy cooling, outer defeated powdery or molding clean coaler Product；

Outer defeated solid thermal carriers, into other powder pyrolytic reaction systems；

Outer defeated solid thermal carriers, can be directly entered dry pulverized coal gasification burner；

4. the semicoke dust that flue gas carries, generally goes through the recycling of flue gas depth dedirt system；

5. burn the undulate quantity of system reserve.

By taking the processing of northern Shensi jet coal fine coal as an example, the riser fine coal heat using oxidation semicoke for high-temp solid heat carrier Solution reactor, pyrolysis char burn system, balance amount of burnt be usually less than pyrolysis char 25% (usually only account for semicoke 8~ 20%), it is remaining be more than 75% pyrolysis char or oxidation semicoke will act as other purposes, that is to say, that balance amount of burnt with Outer is much larger than balance amount of burnt with burnt amount, therefore, amount of burnt is changed discounting for thermal energy, then coke discharge amount is much larger than balance burning Jiao Liang.It is contemplated that if balance amount of burnt burn-up is bulky grain semicoke (its product is flue gas, little particle semicoke) and oxidation Semicoke is mixed into a material, then pyrolysis burns the particle diameter of the solid thermal carriers of system by less than the particle diameter of pyrolysis char；Also may be used To contemplate, if balance amount of burnt burn-up is little particle semicoke (its product is flue gas, more short grained semicoke) and oxidation half Jiao is mixed into a material, then the particle diameter for the solid thermal carriers that system is burnt in pyrolysis will be greater than the particle diameter of pyrolysis char, either Which kind of situation, burning rear particle size distribution has the characteristics that uncertainty is it will be evident that classification coke discharging is manually set in other words Mode, can significantly affect solid material in system (oxidation semicoke i.e. solid thermal carriers, pyrolytic reaction product solid, settler Interior solid, burn solid in device, solid in related gas solid separation step such as cyclone separator) solid particle particle diameter distribution.

However, foregoing CN105602593A, CN105694933A method, carries out without reference to according to grain graininess size Classify coke discharging the problem of, there are solid thermal carriers size controlling ability it is weak the problem of, pulverized coal pyrolysis is burnt in system solid material There is the tendency risen in the reserve and concentration of little particle LS, add the dedirt load of pyrolytic reaction gas-solid product, add heat Solve solids content in tar.

In order to overcome or weaken drawbacks described above, the present invention proposes the hydrocarbon powder pyrolysis of solid heat carrier method and burns system point Class coke discharging method and apparatus.

The present invention it is basic contemplate be：The hydrocarbon powder pyrolysis of solid heat carrier method is burnt genealogical classification coke discharging method and is set It is standby, it is suitable for pulverized coal pyrolysis fluid bed burning process, is burnt in the hydrocarbon powder R10FS pyrolysis using solid thermal carriers R10KS In system UNIT, solid thermal carriers R10KS circulate by arbitrary procedure position, isolate comprising solid thermal carriers At least a portion little particle LS under critical grain size DZ in material EM is simultaneously collected, is discharged recycling, to reduce solid thermal load The concentration of body small particles LS, can significantly reduce pyrolytic reaction gas-solid product dedirt load, reduce pyrolytic tar in solid contain Amount.

It is an object of the present invention to, based on balance the relatively low deoxygenation semicoke ratio outer in other words of amount of burnt ratio it is higher this Part, is the Classification Management that outer row's semicoke implements grain graininess to big flow logistics, realizes to big flow solid circle heat carrier The control of grain graininess, method are categorised collection, discharge and the post-production to different-grain diameter semicoke, and classification coke discharging process includes " classification, collect, discharge " step, wherein classifying step are first steps, and the workflow position of granules step at least can be with The following position of selection：

1. pyrolytic reaction product gas solid separation system S10；

2. it is pyrolyzed settler gas gas solid separation system S20；

3. burn the flue gas gas solid separation system S50 of system；

4. the additional wind screening system AS50 of pyrolysis char.

And in order to simplify equipment and system, improve classification effectiveness, it is contemplated by the invention that being revolved using the wind-force of gas-solid material Divide, FLOTATION SEPARATION is carried out to semicoke particle in grain bed using fluidized wind, and produce corresponding granules scheme.

Based on granules concept, multiple workflow positions, the granules system of diversified forms, principal mode can be set At least：

(1) classification rotation point is carried out using the wind-force of gas-solid material, by the high solid material of little particle LS weight concentrations, little particle The high solid material categorised collection of low i.e. bulky grain concentration of LS weight concentrations or processing, concrete mode have：

1. in pyrolytic reaction product gas solid separation system S10, using 2 grades or multi-cyclone, 2 grades or rear class are revolved The solid material rich in little particle LS of wind separator discharge, introduces little particle semicoke collecting region LS-1W, and can set air lift de-oiling Facility, the little particle semicoke of LS-1W discharges, can be directly entered the little particle coal-char combustion area of burning reaction process R50 or Row's heat exchange it can be stored in addition after cooling down；

2. settler gas gas solid separation system S20 is being pyrolyzed, using 1 grade or 2 grades or multi-cyclone, by whirlwind The solid material rich in little particle LS of separator discharge, introduces little particle semicoke collecting region LS-2W, and air lift de-oiling can be set to set Apply, the little particle semicoke of LS-2W discharges, the little particle coal-char combustion area of burning reaction process R50 can be directly entered or can Stored in addition after row's heat exchange cooling；

In settler is pyrolyzed, height is raised according to dust, vertical peace of the cyclone separator in settler can be adjusted Dress height, can adjust dilute phase bed height at the top of settler in other words, change the particle diameter of solid in whirlwind suction gas-solid material；

3. the flue gas gas solid separation system S50 of device is being burnt, using 1 grade or 2 grades or multi-cyclone, by whirlwind point From the solid material rich in little particle LS of device discharge, little particle semicoke collecting region LS-5W, LS-5W discharge little particle semicoke is introduced；

In device is burnt, height is raised according to dust, it is high that right angle setting of the cyclone separator in settler can be adjusted Degree, can adjust dilute phase bed height at the top of settler in other words, change the particle diameter of solid in whirlwind suction gas-solid material；

4. the additional wind screening system AS50 of pyrolysis char, to pyrolysis char carry out wind-force rotation point classification, using 1 grade or 2 grades or multi-cyclone, the solid material rich in little particle LS that cyclone separator is discharged, introduces little particle semicoke and collects Area LS-6W, LS-6W discharge little particle semicoke；

The additional wind screening system AS50 of pyrolysis char, can be independent system, can be with burning device and burning The united system of smoke processing system, such as：

The first scheme：The additional wind screening system AS50 of independent pyrolysis char, integral arrangement are being burnt inside device, The gas of AS50 discharges enters the solid material rich in little particle LS of flue gas cyclone separation system S50, AS50 discharge, introduces flue gas Little particle semicoke collecting region LS-5W, LS-5W the discharge little particle semicoke of gas solid separation system S50 discharges, AS50 are discharged poor small The bulky grain solid semicoke material of particle LDS, such as burns dense bed space into reaction zone is burnt；

Second scheme：The additional wind screening system AS50 of pyrolysis char combines with flue gas cyclone separation system S50, whole Body, which is arranged in, to be burnt inside device, and at least a portion pyrolysis char is introduced into flue gas cyclone separation system S50, using burning device flue gas Wind-force carry out rotation point, the solid material rich in little particle LD3 of S50 discharges, introducing little particle semicoke collecting region LS-5W, LS-5W Little particle semicoke is discharged, the bulky grain solid semicoke material of the poor little particle LS of S50 discharges, such as burns close phase into reaction zone is burnt Bed space；

(2) FLOTATION SEPARATION is carried out by the high solid of little particle LS weight concentrations to semicoke particle in grain bed using fluidized wind The high solid material categorised collection of low i.e. bulky grain concentration of material, little particle LS weight concentrations or processing, concrete mode have：

1. in settler is pyrolyzed, height is raised according to dust, little particle dust collection groove can be set to receive top empty Between the little particle dust that lands, can set little particle dust collection groove downflow weir baffle receive adjacent space float or overflow into The little particle dust entered；

2. in device is burnt, height is raised according to dust, little particle dust collection groove can be set to receive upper space drop The little particle dust fallen, can set little particle dust collection groove downflow weir baffle receive adjacent space float or overflow enter Little particle dust.

Reaction process is burnt in the pyrolysis that the method for the present invention can be applied to a variety of solid powders containing carbon hydrogen element, can also be answered For 2 kinds or a variety of separate sources powders joint processing.

The method of the invention, has no report.

The first object of the present invention is to propose that genealogical classification coke discharging method is burnt in the hydrocarbon powder pyrolysis of solid heat carrier method And equipment.

The second object of the present invention be propose solid heat carrier method pulverized coal pyrolysis burn system classification coke discharging method and Equipment.

The third object of the present invention is point for proposing that solid heat carrier method pulverized coal fluidized bed pyrolysis fluid bed burns system Class coke discharging method and apparatus.

The content of the invention

Genealogical classification coke discharging method and apparatus is burnt in the hydrocarbon powder pyrolysis of solid heat carrier method of the present invention, it is characterised in that bag Containing following steps：In system UNIT is burnt using the hydrocarbon powder R10FS of solid thermal carriers R10KS pyrolysis, carried in solid thermal Body R10KS circulate by arbitrary procedure position, isolate the critical grain size DZ in the material EM comprising solid thermal carriers Under at least a portion little particle LS and collect, discharge recycling, to reduce the concentration of solid thermal carriers small particles LS.

The present invention, system UNIT is burnt in pyrolysis to be burnt and be reacted by fluid bed riser pyrolytic reaction process and fluidisation Journey R50 is formed：

In system UNIT is burnt using the hydrocarbon powder R10FS of solid thermal carriers R10KS pyrolysis, in solid thermal carriers R10KS circulate by arbitrary procedure position, isolate critical grain size DZ in the material EM comprising solid thermal carriers it Under at least a portion little particle LS and collect, discharge recycling, to reduce the concentration of solid thermal carriers small particles LS；

(1) in level-one pyrolytic reaction process R10, fluid bed riser pyrolysis reactor R10E, hydrocarbon powder are used R10FS, the first solid thermal carriers R10KS are mixed from lower part into reactor R10E, by carrying under gas feed R10FV effects Riser pyrolysis reactor R10E flows up progress level-one pyrolytic reaction R10R and is converted into level-one pyrolytic reaction gas-solid product R10P；

(2) in gas solid separation process S10, level-one pyrolytic reaction gas-solid product R10P by using cyclone separator separation System is separated into level-one pyrolysis coal gas R10PV and level-one pyrolysis char R10PS；

(3) it is anti-into two level pyrolytic reaction process R20's in two level pyrolytic reaction process R20, level-one pyrolysis char R10PS Space is answered, main body flow direction is to flow from above to below, and level-one pyrolysis char R10PS carries out the second pyrolytic reaction R20R；

Two level pyrolysis char R20PS discharge two level pyrolytic reaction processes R20；

(4) in gas solid separation process S20, the pyrolysis coal gas of the dust-laden two level after solid powder main body bed is left, by making The dedirt two level pyrolysis coal gas R20PV of discharge gas solid separation process S20 is separated into the piece-rate system S20 of cyclone separator and is returned Return the reflux semicoke S2PS in two level pyrolytic reaction space；

(5) reaction process R50 is burnt in fluidisation, the final pyrolysis char RCPS based on two level pyrolysis char R20PS enters Fluidisation burns reaction compartment, is contacted with oxygen-containing gas, carries out fluid bed and burns reaction R50R, produces high-temperature oxydation semicoke R50PS With flue gas YQ, flue gas YQ reaction process R50 is burnt from upper space discharge fluidisation；High-temperature semi-coke R50PS discharges fluidisation is burnt instead Answer process R50；

(6) the first high-temperature oxydation semicoke BS1 of R50 discharges is used as the first solid thermal carriers R10KS into riser pyrolysis The lower part of reactor R10E is mixed with fine coal；

(7) the second high-temperature oxydation semicoke BS2 of R50 discharges is used as the second solid thermal carriers SK2, hot with coming from containing for R10E Solve the material of semicoke, before final pyrolysis char is formed Hybrid Heating it, the temperature of the second solid thermal carriers SK2 is higher than being mixed The temperature of compound material, the temperature of the second solid thermal carriers SK2 are less than the temperature of the first solid thermal carriers R10KS.

The present invention, isolates small of at least a portion under the critical grain size DZ in the material EM comprising solid thermal carriers Grain LS, separation scheme can use it is following in 1 or 2 or multiple：

1. scheme K01, is classified with thermal decomposition product cyclone separator；

2. scheme K02, is classified with gas cyclone in settler；

3. scheme K03, little particle LS is collected with collecting tank LS-1W in settler；

4. scheme K04, is classified with device flue gas cyclone separator is burnt；

5. scheme K05, is classified with gas cyclone in device is burnt；

6. scheme K06, little particle LS is collected with collecting tank in device is burnt；

7. scheme K07, send pyrolysis char into flue gas cyclone separator classification.

The present invention, the particle diameter of hydrocarbon powder R10FS：It is usually 0~6 millimeter, generally 0~2 millimeter, hydrocarbon powder R10FS is generally selected from the one or more in following materials,：

1. low rotten fine coal；

2. high rotten fine coal；

3. oil shale powder；

4. oil-sand；

5. other can produce the solid powder containing oil vapour in pyrolytic process.

The present invention, the critical grain size DZ numerical value in the material EM comprising solid thermal carriers, can use it is following in 1：

1. DZ≤5 micron；

2. DZ≤1 micron；

3. DZ≤0.5 micron；

4. DZ≤0.1 micron.

The present invention, common operation target are：

(1) in level-one pyrolytic reaction process R10, gas feed R10FV provides fluidisation power, level-one pyrolytic reaction process At least most of caloric receptivity of R10 is provided by the first solid thermal carriers R10KS；

(4) in gas solid separation process S20, the pyrolysis coal gas of the dust-laden two level after solid powder main body bed is left, by extremely Less gas solid separation, gained dedirt two level pyrolyzing coal are completed using the gas solid separation system S2 of the cyclone separator of 2 grades of serial operations Gas R20PV is discharged from two level pyrolytic reaction process R20 reaction compartments top, and S20 and S10 is at least partly shared.

The present invention, the operation target of usual two level pyrolytic reaction process R20 are：

(3) it is anti-into two level pyrolytic reaction process R20's in two level pyrolytic reaction process R20, level-one pyrolysis char R10PS Space is answered, main body flow direction is to flow from above to below, and level-one pyrolysis char R10PS carries out the second pyrolytic reaction R20R and produces two level heat Coal gas and two level solution pyrolysis char are solved, and completes gas solid separation；The Gas-particle Flows status and appearance of two level pyrolytic reaction process R20 is Dispersion fluidized bed.

The present invention, in general, collecting tank LS-1W collects little particle LS in settler, in settler under collecting tank LS-1W Portion, the tar gas and coal gas for being passed through gas stripping gas LS-1V to be carried in air lift semicoke particle, gas stripping gas flow up eventually enter into it is de- In dirt two level pyrolysis coal gas R20PV.

The present invention, in general, (3) in the lower part of the two level pyrolytic reaction process R20 two level pyrolysis reactor R20E used, lead to The tar gas and coal gas for entering gas stripping gas V22V to be carried in air lift semicoke particle, gas stripping gas, which flows up, eventually enters into dedirt two level It is pyrolyzed in coal gas R20PV.

The present invention, gas stripping gas, can be selected from coal gas or nitrogen and/or vapor and/or anaerobic flue gas.

The present invention, in general, (5) burn reaction process R50 in fluidisation, the final pyrolysis based on two level pyrolysis char R20PS Semicoke RCPS burns reaction compartment into fluidisation, is contacted with the oxygen-containing gas flowed from bottom to top, and fluid bed occurs and burns reaction R50R, produces high-temperature semi-coke R50PS and flue gas YQ, and flue gas YQ burns reaction process R50 from upper space discharge fluidisation；High temperature half Burnt R50PS discharges fluidisation burns reaction process R50.

The present invention, in general, (5) burn reaction process R50 in fluidisation, fluidisation burns the device of the top dilute phase section of reaction compartment Interior ash-laden gas R50E-YQ, the cyclone separation system S5 dedirts for burning the upper space of inside reactor by being arranged in fluidisation It is separated into flue gas YQ and semicoke dust R50-RS；Flue gas YQ leaves cyclone separation system S5 discharges fluidisation from upper space and burns instead Answer process R50.

The present invention, in general, (5) burn reaction process R30 in fluidisation, fluidisation burns the device of the top dilute phase section of reaction compartment Interior ash-laden gas R50E-YQ, the cyclone separation system S5 dedirts for burning the upper space of inside reactor by being arranged in fluidisation It is separated into flue gas YQ and semicoke dust R50-RS；The semicoke dust R50- of the cyclone dip-leg discharge of cyclone separation system S5 RS returns to fluidisation and burns reaction compartment cyclic process.

The present invention, in general, (7) burn reaction process R50 in fluidisation, sets external warmer R50-OUT-HX, discharge fluidisation Burn reaction process R50 hot semicoke enter external warmer R50-OUT-HX and take thermal medium indirect heat exchange reduce temperature after, row Go out external warmer R30-OUT-HX, cooling step XH is completed in heat collector R50-OUT-HX.

The present invention, in general, (7) burn reaction process R50 in fluidisation, sets external warmer R50-OUT-HX, carrys out self-fluidized type The hot semicoke for burning reaction process R50 enters external warmer R50-OUT-HX and takes thermal medium indirect heat exchange to reduce temperature, discharge The hot semicoke of at least a portion of external warmer R50-OUT-HX returns to fluidisation and burns reaction process R50 recyclings, remainder Hot semicoke is used as hot product R50PS-T, and cooling step XH is completed in heat collector R50-OUT-HX.

The present invention, in general, (7) burn reaction process R50 in fluidisation, sets external warmer R50-OUT-HX, carrys out self-fluidized type The hot semicoke for burning reaction process R50 enters external warmer R50-OUT-HX and takes thermal medium indirect heat exchange to reduce temperature, discharge The hot semicoke of Part I of external warmer R50-OUT-HX returns to fluidisation and burns reaction process R50 recyclings, and Part II is cold But it is used as product R50PS-C afterwards, cooling step XH is completed in heat collector R50-OUT-HX.

The present invention, in general, two level pyrolysis reactor is also settler at the same time.

The present invention, R10, R20 operation target are usually：

(1) in level-one pyrolytic reaction process R10, the particle diameter of hydrocarbon powder R10FS is 0~6 millimeter, hydrocarbon powder R10FS Low rotten fine coal selected from high volatile；

(3) the tar steam weight that two level pyrolytic reaction process R20 is produced is the 1~12% of fresh fine coal R10FS weight；

The coke breeze R20PS volatilizations of two level pyrolytic reaction process R20 are divided into 3~25%；

The tar yield of level-one pyrolytic reaction process R10 is R10PY, the tar yield of two level pyrolytic reaction process R2 is R20PY is with defining KR=R20PY/ (R10PY+R10PY), KR is 0.05~0.50.

The present invention, R10, R20 operation target are generally：

(1) in level-one pyrolytic reaction process R10, the particle diameter of hydrocarbon powder R10FS is 0~6 millimeter, hydrocarbon powder CHLS choosings From the low rotten fine coal of high volatile；

(3) the tar steam weight that two level pyrolytic reaction process R20 is produced is the 1~7% of fresh fine coal R10FS weight；

The coke breeze R20PS volatilizations of two level pyrolytic reaction process R20 are divided into 3~15%；

KR is 0.05~0.30.

The present invention, each step operation target are usually：

(1) in level-one pyrolytic reaction process R10, the R10FS of powder containing carbon hydrogen element is fine coal；

Level-one pyrolytic reaction process R10, using riser fluidized bed pyrolysis reactor, the first solid thermal carriers R10KS is Carry out the high-temperature oxydation semicoke that self-fluidized type burns reaction process R50；

The operating condition of level-one pyrolytic reaction process R10 is：0.1~10s of reaction time, riser reacting product outlet temperature Degree is that level-one pyrolytic reaction process cessation reaction temperature is 400~500 DEG C；

The weight of first solid thermal carriers R10KS is 1~30 with fine coal R10FS weight ratios；

(2) solids content is less than 50 grams/cubic metre in gas solid separation process S10, dedirt level-one pyrolysis coal gas R10PV；

(3) in the reaction compartment of two level pyrolytic reaction process R20,2~12 secondary herringbone baffles or ring baffle, two level are set The temperature of the main pyrolysis section of pyrolytic reaction process is 460~700 DEG C；

Two level pyrolysis section bottom is passed through 450~650 DEG C of gas stripping gas V22V and carries out tar steam stripping, and gas stripping gas V22V passes through Flow up after the semicoke bed of material and be pyrolyzed into the two level of two level pyrolytic reaction process R20 in coal gas product；

Weight into the second solid thermal carriers SK2 of two level pyrolytic reaction process R20 is with fine coal R10FS weight ratios 0.3~10；

(4) in the gas solid separation process S20 of second level pyrolytic reaction gas-solid product, two level pyrolysis coal gas product is by thick rotation All gaps between being revolved with top enter top whiz and open two level pyrolytic reaction space, and on top, medial rotation is with the first pyrolytic reaction gas-phase product First pyrolysis coal gas is mixed into row gas solid separation.

The present invention, each step operation target are generally：

(1) in level-one pyrolytic reaction process R10, the R10FS of powder containing carbon hydrogen element is low rotten fine coal；

The operating condition of level-one pyrolytic reaction process R10 is：1.0~6s of reaction time, riser reacting product outlet temperature Degree is that level-one pyrolytic reaction process cessation reaction is 430~470 DEG C；

The weight of first solid thermal carriers R10KS is 3~15 with fine coal R10FS weight ratios；

(2) in gas-solid gas solid separation process S10, in a dedirt level-one pyrolysis coal gas R10PV solids content less than 10 grams/it is vertical Square rice；

(3) in the reaction compartment of two level pyrolytic reaction process R20,2~12 secondary herringbone baffles or ring baffle, two level are set The temperature of the main pyrolysis section of pyrolytic reaction process is 480~600 DEG C；

Weight into the second solid thermal carriers SK2 of two level pyrolytic reaction process R20 is with fine coal R10FS weight ratios 1.0~5；

The present invention, each step operation target preferably are：

(1) in level-one pyrolytic reaction process R10, the R10FS of powder containing carbon hydrogen element is the low rotten fine coal of high volatile；

The operating condition of level-one pyrolytic reaction process R10 is：2.5~4s of reaction time, riser reacting product outlet temperature Degree is that level-one pyrolytic reaction process cessation reaction is 440~460 DEG C；

The weight of first solid thermal carriers R10KS is 6~10 with fine coal R10FS weight ratios；

(2) solids content is less than 4 grams/cube in gas-solid gas solid separation process S10, dedirt level-one pyrolysis coal gas R10PV Rice；

(3) in the reaction compartment of two level pyrolytic reaction process R20,2~12 secondary herringbone baffles or ring baffle, two level are set The temperature of the main pyrolysis section of pyrolytic reaction process is 480~530 DEG C；

Weight into the second solid thermal carriers SK2 of two level pyrolytic reaction process R20 is with fine coal R10FS weight ratios 2~3；

The present invention, the riser fluidized bed pyrolysis reactor R10E that level-one pyrolytic reaction process R10 is used are pyrolyzed with two level The two level fluidized bed pyrolysis reactor R20E that reaction process R20 is used, can form unit equipment.

The present invention, the two level fluidized bed pyrolysis reactor R20E that two level pyrolytic reaction process R20 is used are burnt instead with fluidisation The fluid bed that the process R50 of answering is used burns reaction process R50E, can form unit equipment.

The present invention, riser fluidized bed pyrolysis reactor R10E that level-one pyrolytic reaction process R10 is used, two level pyrolysis are anti- Two level fluidized bed pyrolysis reactor R20E that the process R20 of answering is used, fluidisation are burnt the fluid bed that reaction process R50 is used and are burnt instead Process R50E is answered, unit equipment can be formed.

The present invention, the two level fluidized bed pyrolysis reactor R20E that two level pyrolytic reaction process R20 is used, fluidisation burn reaction It is vertical equipment that the fluid bed that process R50 is used, which burns reaction process R50E, and from locus, absolute altitude is said, its mutual alignment is closed It is to be：The bottom that fluid bed burns reactor R50E is lower than the bottom of two level pyrolysis apparatus R20E, two level pyrolysis apparatus R20E The final pyrolysis char of discharge burns the bottom of reactor R50E by material position difference inflow fluid bed.

The present invention, the two level fluidized bed pyrolysis reactor R20E that two level pyrolytic reaction process R20 is used, burns instead with fluidisation The fluid bed that the process R50 of answering is used burns reaction process R50E, can form coaxial-type unit equipment；

It is coaxial-type Vertical Combination that coaxial-type, which refers to that two level pyrolysis reactor R20E, fluid bed burn reactor R50E, Equipment, says from spatial relation, its mutual alignment relation is：Fluid bed surrounds with burning the space segment of reactor R50E The space of two level pyrolysis apparatus R20E；The pyrolysis char of bottom space from two level pyrolysis apparatus R20E is flowed into by standpipe and plug valve Fluid bed burns the lower space of reactor R50E.

The present invention, the operating pressure of each reactions steps are usually：

(1) operating pressure of level-one pyrolytic reaction process R10 is：0.1~6.0MPa, with absolute manometer；

(3) operating pressure of two level pyrolytic reaction process R20 is：0.1~6.0MPa, with absolute manometer；

(5) operating pressure that fluidisation burns reaction process R50 is：0.1~6.0MPa, with absolute manometer.

Brief description of the drawings

Fig. 1 is the flow function signal for the classification coke discharging method that the hydrocarbon powder solid heat carrier pyrolysis of the present invention burns system Figure, at the same be a kind of fine coal riser fluidized bed pyrolysis, pyrolysis char fluidisation burn, solid thermal carriers circulation, classification coke discharging The hydrodynamics view of solid material circulating path, for representing the work(of each workflow position in pulverized coal pyrolysis burning process Energy.

Fine coal riser fluidized bed pyrolysis fluid bed as shown in Figure 1 burns system, including fine coal riser fluid bed heat Solution reactor, settler i.e. the second pyrolysis reactor, the fluid bed of pyrolysis char burn reactor, and the wherein top of settler is empty Between be disposed with the cyclone separator of separation coal gas and semicoke, wherein fluid bed burns the upper space of reactor and is disposed with separation cigarette The cyclone separator of gas and semicoke.

Said from the hydrodynamics state aspect of solid material circulating path, the function layout of flow shown in Fig. 1 is：Conventional " uplink (level-one pulverized coal pyrolysis riser reactor), bottom horizontal flow sheet (level-one pulverized coal pyrolysis reaction product gas solid separation), downlink (level-one pyrolysis char is in cyclone dip-leg, two level pulverized coal pyrolysis reaction compartment), pyrolysis char Solid Conveying and Melting, fluid bed Burn, solid thermal carriers conveying ", collectively constitute 0 shape circuit.

As shown in Figure 1, in 0 shape circuit, classification coke discharging is performed to pyrolysis char, can obtain bulky grain oxidation semicoke, Little particle aoxidizes semicoke, and can control the particle diameter distribution of solid thermal carriers as needed；The method of classification coke discharging is at least：

1. scheme K01, is classified with thermal decomposition product cyclone separator, collected, discharge；

2. scheme K02, is classified with gas cyclone in settler, collected, discharge；

3. scheme K03, is collected, discharge with collecting tank in settler；

4. scheme K04, with burn device flue gas cyclone separator classify, collect, discharge；

5. scheme K05, is classified, is collected, discharge with gas cyclone is burnt in device；

6. scheme K06, with burn in device collecting tank collect, discharge；

7. scheme K07, send pyrolysis char into flue gas cyclone separator classification, collects, discharge；

8. selection scheme K01 is into scheme K07, the efficient combination scheme of 2 kinds or kinds of schemes.

As shown in Fig. 2, the classification coke discharging mode of the little particle collecting tank LS-1W of settler R20E inner spaces arrangement, is The combination of tri- kinds of schemes of K01, K02, K03.

As shown in figure 5, burn device R50E inner spaces arrangement little particle collecting tank classification coke discharging mode, be K04, The combination of tetra- kinds of schemes of K05, K06, K07.

Fig. 2 is the functions of the equipments schematic diagram for the classification coke discharging method that system is burnt in a kind of pulverized coal fluidized bed pyrolysis of the present invention, Settler R20E is height block form with burning device R50E, for representing the stream of classification coke discharging system in pulverized coal pyrolysis burning process Journey position and device structure.

Fig. 2 is that height block form pulverized coal pyrolysis burns system；Height block form refers to that settler R20E, fluid bed are burnt Burnt reactor R50E is vertical equipment, and from locus, absolute altitude is said, its mutual alignment relation is：Fluid bed burns reactor The bottom of R50E is lower than the bottom of settler R20E, and the final pyrolysis char of settler R20E discharges can rely on material position difference gravity flow The bottom of reactor R50E is burnt into fluidized bed.Settler R20E, because having the function of necessarily pyrolysis, alternatively referred to as two level is hot Solve reactor.

As shown in Fig. 2, R10E is lifting tubular type level-one pyrolysis reactor, lifting gas R10FV enters through pipeline P101 to be arranged Flowed up after the distributor R10FV-SB distribution of R10E bottoms, fine coal FM (i.e. R10FS) is through pipeline P102, the first solid thermal Carrier semicoke R10KS through pipeline P103 enter R10E bottoms mixed zone R10E-1 lifting gas R10FV effect under form fluid bed Moved up along riser, the first pyrolytic reaction of fine coal R10R during which occurs；Heat transfer path has heat carrier semicoke → fine coal, height Warm fine coal → low temperature fine coal, heat carrier semicoke → gas, high-temperature gas → cryogenic gas, high-temperature gas → fine coal, high frequency time Mixing, separation form flash heat transfer effect, and fine coal carries out level-one pyrolytic reaction in temperature-rise period；Complete the first pyrolytic reaction Material discharges R10E as the first pyrolytic reaction effluent R10P from open top R10E-OUT, and R10P is by comprising tar component Coal gas, pyrolysis char composition gas-solid mixed phase logistics.

As shown in Fig. 2, level-one pyrolytic reaction effluent R10P enters thick rotation S101 through pipe P105, the thick S101 that revolves completes level-one Gas solid separation.

As shown in Fig. 2, segregation section S10 is the gas solid separation system of level-one pyrolytic reaction effluent R10P, sedimentation is arranged in The tip position of device R20E inner spaces.

Fig. 3 is the thtee-stage shiplock separation process detail drawing of the gas solid separation system S10 in Fig. 2, and the thick S101 that revolves separates for level-one, The main rotation S102 of level-one is the second-order separation, and the main rotation S103 of two level separates for three-level.

The connection mode signal that Fig. 4 is the thick rotation S101 and main rotation S102 of level-one of the gas solid separation system S10 in Fig. 3 is detailed Figure.As shown in figure 4, slightly there is all gaps between rotation S101 exit gas conveyance conduit and the gas feed mouth of main rotation, as reception The feed inlet of the dust-laden coal gas of settler R20E.

As shown in figure 3, level-one pyrolytic reaction effluent R10P enters thick rotation S101 through pipe P105, the thick S101 that revolves completes level-one Gas solid separation, it is thick revolve powder lower into settler R20E inner spaces along dipleg P106 and typically flow into dense bed region to prevent Only dust is excessively flown upward；Thick rotation coal gas containing dust sprays into the feed pipe P108 for the main rotation S102 of level-one being flexible coupling along pipe P107, The main rotation S102 of level-one completes two level gas solid separation, and the main rotation powder of level-one lowers into settler R20E inner spaces along dipleg P109 And dilute-phase leanphase fluidized bed region is typically flowed into, the main rotation powder of at least a portion level-one lowers into empty inside settler R20E along dipleg P109 Between the little particle collecting tank LS-1W that arranges；The main rotation coal gas of level-one containing a small amount of dust enters the two level being directly connected to along pipe P111 Main rotation S103, the main rotation S103 of two level complete three-level gas solid separation, and the main rotation powder of two level lowers into settler along dipleg P112 R20E inner spaces simultaneously typically flow into dilute-phase leanphase fluidized bed region, and the main rotation powder of at least a portion two level lowers into sedimentation along dipleg P112 The little particle collecting tank LS-1W of device R20E inner spaces arrangement；The main rotation coal gas of dedirt two level is as one section of separation coal gas S10PV edge Pipe P115 discharge systems S10.

As shown in figure 4, in segregation section S10, the thick rotation coal gas containing dust sprays into the main rotation of level-one being flexible coupling along pipe P107 The feed pipe P108 of S102, Fig. 4 illustrate one kind and are flexible coupling mode, and the head of feed pipe P108 is that an expanding horn mouth opens Mouthful P1081, the head P1071 of pipe P107 are one and extend into the sky of horn mouth P1081 with footpath extension opening P1071, P1071 In, there is all gaps between thick screw outlet gas transmission pipeline and the gas feed mouth of pipe of main rotation.

As shown in Fig. 2, R20E is two level pyrolysis reactor, the inner space of R20E, includes at least according to process function and sets Put the headroom V21 of cyclone separation system, one section of sedimentation degassing space or two level pyrolytic reaction space for separating semicoke S10PL V22, little particle collecting tank LS-1W.

It is generally desirable to two level pyrolytic reaction space present particulate fluidization bed form, at this time, top for dilute phase space V21, under Portion is close phase space V22, and close phase space V22 bottoms usually have stripping gas V22V to flow up.

As shown in Fig. 2, the coke breeze in the dipleg of system S10 enters two level pyrolytic reaction process R20, i.e. whirlwind by gravity Coke breeze in separator dipleg enters the space of two level pyrolysis reactor R20E by gravity.

As shown in Fig. 2, one section into settler R20E reaction compartments V22 separates semicoke S10PL, producing main body flow direction is Simultaneously flow direction is varied multiple times by baffle in top-down flowing, the structure type of baffle have a variety of such as setting polylith herringbone baffles, Polylith annular slab etc., separates the second pyrolytic reaction R20R of semicoke S10PL progress for one section in above process；It is anti-to complete two level pyrolysis The material answered is divided into the two level pyrolysis char R20EPS and two level pyrolysis dust-laden coal gas R20EPV of downlink, two level pyrolysis half after degassing Burnt R20PS is discharged from the bottom of settler R20E reaction compartments through pipeline P302, valve, pipeline P502, two level pyrolysis char R20PS may finally go fluid bed to be stored after burning reactor R50E or cooling.

As shown in Fig. 2, in settler R20E, at least a portion little particle semicoke is collected in little particle collecting tank LS-1W In, discharged through pipeline P351, valve, pipeline P352；Little particle collecting tank LS-1W bottoms, are usually passed through 450~650 DEG C of air lifts Gas LS-1V enters collecting tank LS-1W bottoms, air lift after entering in R20E the distributor LS-1V-SB distribution arranged along pipeline P355 Gas is by air lift after the semicoke bed of material and carries the two level that tar steam flows up and eventually enter into two level pyrolytic reaction process R20 It is pyrolyzed in coal gas product.

Fig. 5 is that the fluid bed in Fig. 2 burns the detail of construction that the fluid bed that system R50 is used burns reactor R50E, is burnt It is small that top flue gas cyclone separation system S50, bottom dense bed scorch region VA52, bottom dense bed are disposed with burnt reactor R50E Particle collection trough VB52 (can also be arranged as scorch region).

As shown in figure 5, segregation section S50 is the three-level gas solid separation system of flue gas, it is arranged in and burns device R50E inner spaces Tip position.Meanwhile segregation section S50 is the cyclone separation system of a part of pyrolysis char SX100, a part comes from settler The pyrolysis char SX100 of R20E, enters cyclone separator S501 through pipeline P551, and S501 completes flue gas level-one gas solid separation, and one Rotation separation powder is lowered into along dipleg P555 to be burnt device R50E inner spaces and typically flows into dense bed region VA52 to prevent Dust is excessively flown upward；A rotation flue gas containing dust enters two level whirlwind S502 along pipe P558 and completes two level gas solid separation, two rotation powder Material is lowered into along dipleg P562 to be burnt device R50E inner spaces and typically flows into dilute-phase leanphase fluidized bed region, and at least a portion two revolves powder The little particle collecting tank VB52 for burning device R50E inner spaces arrangement is lowered into along dipleg P562；The two rotation flue gas edges containing dust Pipe P561 enters three-level whirlwind S503 and completes three-level gas solid separation, and three rotation powders are lowered into along dipleg P508 to be burnt in device R50E Portion space simultaneously typically flows into dilute-phase leanphase fluidized bed region, and at least a portion three is revolved powder and lowered into along dipleg P508 and burnt inside device R50E The little particle collecting tank VB52 of space layout, dedirt three revolve flue gas as dedirt flue gas YQ along pipe P507 discharge systems R50E.

Fig. 6 is the detail drawing of the part-structure for burning reactor shown in Fig. 5.

Fig. 6 illustrates the connection mode of the feed entrance pipe of the primary cyclone of the gas solid separation system S50 in Fig. 5 Schematic detail view.S501 feed pipe detail drawings as shown in Figure 6, pyrolysis char SX100 conveyance conduits P551 with one revolve the gas of S501 into There is all gaps between expects pipe P553, as the feed inlet for receiving the ash-laden gas for burning device R50E inner spaces.

As shown in Figure 5, Figure 6, the lower space of reactor R50E is being burnt, being partitioned into two scorch regions, (or one burn Area, little particle semicoke collect discharge region) dense bed space 4 and 6, two scorch regions set respectively burning wind passage and point Cloth device, the public flue gas gas-solid separator of top flue gas of two scorch regions only set a set of gas solid separation system, two close phases Each discharge oxidation semicoke and be used as solid thermal carriers or product in bed space；At least partially, it is typically most of even whole Pyrolysis char enters the first scorch region dense bed 4, the flue gas and the second scorch region dense bed 6 of the discharge of the first scorch region dense bed 4 The flue gas (or fluidized gas) of discharge enters in the lump to be burnt dilute-phase leanphase fluidized bed at the top of reactor R50E and enters cyclone separation system S50, extremely The little particle semicoke that a few part is usually all discharged by cyclone separation system dipleg is burnt into the second scorch region dense bed 6 (or enter the little particle semicoke and collect discharge region)；The little particle semicoke floatingly selected at the top of first scorch region, 4 dense bed can overflow Flow to 6 dense bed of the second scorch region.

As shown in Figure 5, Figure 6, reactor R50E is burnt, its underpart will burn reactor bottom equipped with vertical arc-shaped partition 3 Part is 4 and 6 two parts, and 6 parts can be circular, oval or square；Partition plate 3 is equipped with downflow weir 8, and downflow weir 8 to the greatest extent may be used Can be away from pyrolysis char inlet tube and oxidation semicoke outlet；Pyrolysis char by pipeline P502 from burn reactor bottom or A section dense bed space 4 is burnt into first in side (as shown in Figure 5)；First burns the oxidation semicoke outlet of section dense bed 4 One flange 19 is arranged at 18 tops, burns section bottom in dense bed space 4 positioned at first；Second burns the oxidation semicoke of section dense bed 6 One flange 24 is arranged at 23 top of outlet, burns section bottom in dense bed space 6 positioned at second；First, which burns wind, passes through inlet tube 29 Into air sparger 26；May use second burns wind and enters air sparger 27 by inlet tube 31；Partition plate 3 and burn The connection mode of wall of reactor should ensure that avoids weld cracking under the conditions of various operation operating modes, prevents the deformation of partition plate 3 from making Burnt into two and semicoke short circuit is formed between section dense bed；Two semicoke circulation conveyings burnt between section dense bed form partition plate The notch overflow at top, can mutually convey the solid particle at the top of bed, realize that material position is adjusted, adaptation is burnt, coke discharging of classifying Process control.By regulating and controlling oxidation semicoke external warmer thermic load and burning the burning air quantity of reactor, can neatly adjust Ratio of making charcoal is saved, realizes that controlling is made charcoal, obtains needing the oxidation semicoke solid thermal carriers or product of particle diameter distribution.

As shown in Fig. 2, Fig. 5, reactor R50E is burnt in fluid bed, the final pyrolysis char such as two from settler R20E Level pyrolysis char R20PS, enter after piping P302, valve, pipeline P502 burn reactor R50E burn a section dense bed In VA52, that is, space 4, oxygenous lifting gas VA52-ZF, which enters, to be arranged in after the distributor VA52-SB distributions of 4 bottom of space upwards Flowing, forms semicoke fluidized bed combustion, the flue gas of generation of burning burnt along fluid bed SPACE V A52 in reactor R50E, V51 is moved up and is carried semicoke dust secretly.

As shown in Fig. 2, Fig. 5, fluid bed burns burning for reactor R50E and flue gas VA50EPV is burnt in the device of section, its gas Solid separation process S50 is arranged in the tip position that fluid bed burns reactor R50E inner spaces, by 1 grade of cyclone separator or string 2 grades or multi-cyclone composition of connection operation, are shown in the figure the scheme of 3 grades of cyclone separator serial operations.Gas-solid Separation process S50, gained dedirt flue gas YQ burns reactor R50E through pipeline P507 discharge fluid beds and goes to press after separating coke breeze Power can recycle and/or heat recovery and/or the processing of dust depth piece-rate system, and usually flue gas YQ is discharged into air after processing or part is followed Ring utilizes；Gas solid separation process S50, the coke breeze R50-KR in separator dipleg return to fluid bed by gravity and burn reactor In R50E.

As shown in Fig. 2, semicoke is aoxidized by the bulky grain of pipeline P503, guiding valve and pipeline P103 conveying, as solid thermal Carrier R10KS enters level-one pyrolysis reactor R10E.

As needed, other hot semicoke discharge fluid beds burn reactor R50E, storage or direct after the cooling that can exchange heat Gasification etc. is burnt or is directly used in for firing process.

As shown in Fig. 2, one section of separation coal gas S10PV enters later separation recovery system S30 by pipeline P115.

Fluid bed as shown in Figure 5 burns reactor R50E, its device headspace can arrange indirect heat exchanger R50E- HX, takes hot logistics such as recirculated water to heat gas phase or liquid phase or mixed phase, treats overheated steam, gas stream etc..

In Fig. 5, distributor R10FV-SB or V22V-SB or VA525-SB or VB525-SB or LS-1V-SB, can be any Suitable form, for example can be the nozzle of head cover for being provided with multiple apertures or be an annular spread for being provided with multiple apertures Pipe or the nozzle chamber for a head cover for being provided with multiple apertures.

As shown in Fig. 2, two level is pyrolyzed dust-laden coal gas R20EPV, its gas solid separation process S20 is flowed out with level-one pyrolytic reaction The gas solid separation section S10 of thing, can partly or entirely share main rotation system, receive the feed inlet of two level pyrolysis dust-laden coal gas R20EPV For " all gaps between thick screw outlet gas transmission pipeline and the gas feed mouth of main rotation ", two level be pyrolyzed dust-laden coal gas R20EPV from Open the main precession row gas solid separation that two level pyrolytic reaction space enters system S10.

As shown in Fig. 2, 450~650 DEG C of gas stripping gas V22V enter in V22 the distributor V22V-SB arranged along pipeline P2201 Enter 22 bottom of two level pyrolytic reaction SPACE V after distribution, gas stripping gas is by air lift after the semicoke bed of material and to carry tar steam upward The two level for flowing and eventually entering into two level pyrolytic reaction process R20 is pyrolyzed in coal gas product.

A kind of hydrocarbon powders flowing purification bed pyrolysis of the present invention is burnt the classification coke discharging method of system and its is set as shown in Figure 2 It is standby, the purpose of classification coke discharging is realized, any suitable location of system is burnt in the pyrolysis of hydrocarbon powders flowing purification bed, in cyclonic separation Device such as in pyrolytic reaction product gas solid separation system S1 and/or pyrolysis settler gas gas solid separation system S2 and/or burns and is Cyclonic separation classification is carried out in the flue gas gas solid separation system S3 of the system or additional wind screening system AS4 of pyrolysis char, or The position with wind-force flotation effect such as settler middle and upper part, burn reactor middle and lower part set coke breeze collecting tank divided Class is collected, and is so separated and/or is collected out the little particle under the expection particle size range in the solid material EM of pyrolytic reaction process Simultaneously discharge system recycles it to LS.

Embodiment

(7) the second high-temperature oxydation semicoke BS2 of R50 discharges is used as the second solid thermal carriers SK2, hot with coming from containing for R10E Solve the material of semicoke, before final pyrolysis char is formed Hybrid Heating it, the temperature of the second solid thermal carriers SK2 is higher than being mixed The temperature of compound material, the temperature of the second solid thermal carriers SK2 are less than the temperature of the first solid thermal carriers R10KS；

2. scheme K02, is classified with gas cyclone in settler；

4. scheme K04, is classified with device flue gas cyclone separator is burnt；

5. scheme K05, is classified with gas cyclone in device is burnt；

1. low rotten fine coal；

2. high rotten fine coal；

3. oil shale powder；

4. oil-sand；

1. DZ≤5 micron；

2. DZ≤1 micron；

3. DZ≤0.5 micron；

4. DZ≤0.1 micron.

The present invention, common operation target are：

The present invention, in general, (7) burn reaction process R50 in fluidisation, sets external warmer R50-OUT-HX, carrys out self-fluidized type The hot semicoke for burning reaction process R50 enters external warmer R50-OUT-HX and takes thermal medium indirect heat exchange to reduce temperature, discharge The hot semicoke of Part I of external warmer R50-0UT-HX returns to fluidisation and burns reaction process R50 recyclings, and Part II is cold But it is used as product R50PS-C afterwards, cooling step XH is completed in heat collector R50-OUT-HX.

The present invention, R10, R20 operation target are usually：

The present invention, R10, R20 operation target are generally：

KR is 0.05~0.30.

The present invention, each step operation target are usually：

The present invention, each step operation target are generally：

The present invention, each step operation target preferably are：

Each step specific features are described below in conjunction with overall procedure.

Into fine coal FM, that is, R10FS of level-one pyrolytic reaction process R10, fine coal is dehydrated after usually drying, its moisture weight Amount usually less than 10%, generally below 7%, preferably are less than 5%.

Into fine coal FM, that is, R10FS of level-one pyrolytic reaction process R10, its granularity is usually 0.00001~6 millimeter, one As for 0.0001~3.5 millimeter, preferably be 0.001~2 millimeter.

Can be any one temperature, pressure, component composition into the gas stripping gas R10FV of level-one pyrolytic reaction process R10 Etc. suitable gas, it is usually vapor or nitrogen or not oxygenous flue gas or purifies coal gas or producing synthesis gas from coal after de-oiling Or semicoke preparing synthetic gas.

Into the first solid thermal carriers SK1 of level-one pyrolytic reaction process R10, usually burn and reacted from fluid bed The high-temperature oxydation semicoke of journey R50, the ratio of its weight flow and fine coal R10FS weight flows, determines as needed, is usually 0.5~30, it is 5~10 to be generally 3~15, preferably.

Level-one pyrolytic reaction process R10, the Type of equipment of the level-one pyrolysis reactor R10E used determine as needed, lead to Often using lifting tubular type level-one pyrolysis reactor.

Gas solid separation section S1, usually using centrifugation formula gas-solid separation equipment element, can form 1 grade or 2 grades or more The gas solid separation system of level serial operation.

In level-one pyrolysis coal gas R10PV solids content be usually less than 50 grams/cubic metre, generally below 10 grams/cubic metre, compared with Good person is less than 4 grams/cubic metre.

Two level pyrolytic reaction process R20, its Type of equipment determine as needed, usually using vertical downflow system settler R20E。

The gas stripping gas of two level pyrolysis reactor bottom, generally selects inert gas such as steam or nitrogen or the flue of no oxygen Gas or purification coal gas circulating air or other inert gases.

On settler R20E structures, its process function is to form fluid bed, preferably form dispersion fluidized bed and expand Bed, the inner space of settler R20E is broadly divided into three sections：Epimere is that the gas of low gas velocity takes off solid space, stage casing is that gas velocity is suitable Two level pyrolysis main reaction space, hypomere be stripping section.

Epimere takes off solid space for the gas of low gas velocity, and therefore, it is necessary to reduce the coal gas in pyrolysis main reaction space from below Cross sectional flow rate, that is to say, that it is required that reducing gas flow rate needs enlarged cross section area, therefore, usual epimere, that is, gas takes off solid The radial section product in space is more than the radial section product in stage casing, that is, two level pyrolysis main reaction space.

Stage casing is pyrolyzed main reaction space for the suitable two level of gas velocity, here, two level pyrolytic reaction occurs for level-one pyrolysis char Discharge coal gas, tar steam；During level-one pyrolysis char is pyrolyzed main reaction space through two level from top to down, with The rise of temperature, level-one pyrolysis char progressively discharge coal gas, tar steam, and two level is pyrolyzed the half of the bottom discharge in main reaction space Burnt release coal gas, the ability of tar steam very little.

In stripping section, the gas stripping gas flowed up of two level pyrolysis reactor lower part stripping section is entered from bottom, it is usually logical Cross gas distributor and realize being uniformly distributed for initial stage, since the effect of the gas is carried in the semicoke of two level pyrolysis reaction section bottom Comprising tar gas, therefore, the flow of gas stripping gas is typically less, says that gas stripping gas belongs to from follow-up coal gas processing and utilization angle Invalid component (vapor, nitrogen, flue gas) or circulating gas, its quantity should reduce as far as possible, the area of section of such stripping section It is usually smaller.In fact, the area of section of stripping section is typically smaller than the area of section in two level pyrolysis main reaction space.

Solids content is usually less than 50 in dedirt two level pyrolysis the coal gas S20V or R20PV of discharge gas solid separation system S20 Gram/cubic metre, generally below 10 grams/cubic metre, preferably are less than 4 grams/cubic metre.

Gas stripping gas V22V, can be the suitable gases such as any one temperature, pressure, component composition, be usually vapor Or coal gas or producing synthesis gas from coal or semicoke preparing synthetic gas after nitrogen or not oxygenous flue gas or purification de-oiling.

Fluid bed burns reaction process R50, and the Type of equipment that fluid bed burns reactor R50E determines as needed, usually Reactor R50E is burnt using vertical fluidized bed.

As needed, fluid bed burns reaction process R50, can discharge thermal oxide semicoke R50PS products or not discharge heat Aoxidize semicoke R50PS products；The thermal oxide semicoke R50PS of discharge is stored after recycling thermal energy being cooled down by indirect heat exchanger.

As needed, fluid bed burns reaction process R50, can set cyclic oxidation semicoke logistics R50RS heat collectors, follow Epoxidation semicoke logistics R50RS burns reaction by returning to fluid bed after defeated thermal energy cooling outside indirect heat exchanger such as steam generator Process R50, at this time, cyclic oxidation semicoke logistics R50RS serve as the heat carrier of outer defeated thermal energy.

As shown in Figure 1, lifting tubular type level-one pyrolysis reactor, can be on similarly hereinafter diameter cylinder riser, can To be not isometrical riser that top large diameter cylinder, middle transition centrum, lower small diameter cylinder form, transition centrum Position can arrange the distributor of the second solid thermal carriers SK2.

The advantage of the invention is that：

1. the reserve and concentration of Efficient Cycle solid thermal carriers small particles LS is capable of in classification coke discharging, it is anti-to significantly reduce pyrolysis Answer the dedirt load of gas-solid product, reduce solids content in pyrolytic tar, beneficial to the steady behaviour of pyrolysis coal gas post-production process Make, beneficial to reduce pyrolytic tar difficulty of processing, improve its utilization rate；

2. kinds of schemes, preferred for detailed process combination specific requirement；

3. it is adapted to new device or existing apparatus transformation.

Claims

1. genealogical classification coke discharging method and apparatus is burnt in the hydrocarbon powder pyrolysis of solid heat carrier method, it is characterised in that includes following step Suddenly：In system UNIT is burnt using the hydrocarbon powder R10FS of solid thermal carriers R10KS pyrolysis, followed in solid thermal carriers R10KS Circulation moves the arbitrary procedure position of process, isolates under the critical grain size DZ in the material EM comprising solid thermal carriers at least A part of little particle LS is simultaneously collected, is discharged recycling, to reduce the concentration of solid thermal carriers small particles LS.

2. method and apparatus according to claim 1, it is characterised in that：

In system UNIT is burnt using the hydrocarbon powder R10FS of solid thermal carriers R10KS pyrolysis, in solid thermal carriers R10KS Circulate by arbitrary procedure position, isolate under the critical grain size DZ in the material EM comprising solid thermal carriers extremely Few a part of little particle LS is simultaneously collected, is discharged recycling, to reduce the concentration of solid thermal carriers small particles LS；

(1) in level-one pyrolytic reaction process R10, fluid bed riser pyrolysis reactor R10E, hydrocarbon powder R10FS, are used One solid thermal carriers R10KS is mixed from lower part into reactor R10E, is pyrolyzed under gas feed R10FV effects by riser Reactor R10E flows up progress level-one pyrolytic reaction R10R and is converted into level-one pyrolytic reaction gas-solid product R10P；

(2) in gas solid separation process S10, level-one pyrolytic reaction gas-solid product R10P by using cyclone separator piece-rate system It is separated into level-one pyrolysis coal gas R10PV and level-one pyrolysis char R10PS；

(3) it is empty in two level pyrolytic reaction process R20, the reaction of level-one pyrolysis char R10PS into two level pyrolytic reaction process R20 Between, main body flow direction is to flow from above to below, and level-one pyrolysis char R10PS carries out the second pyrolytic reaction R20R；

(4) in gas solid separation process S20, the pyrolysis coal gas of the dust-laden two level after solid powder main body bed is left, by using rotation The piece-rate system S20 of wind separator is separated into dedirt two level pyrolysis coal gas R20PV and the return two of discharge gas solid separation process S20 The reflux semicoke S2PS in level pyrolytic reaction space；

(5) reaction process R50 is burnt in fluidisation, the final pyrolysis char RCPS based on two level pyrolysis char R20PS enters fluidisation Reaction compartment is burnt, is contacted with oxygen-containing gas, fluid bed is carried out and burns reaction R50R, produce high-temperature oxydation semicoke R50PS and cigarette Gas YQ, flue gas YQ burn reaction process R50 from upper space discharge fluidisation；High-temperature semi-coke R50PS discharges fluidisation, which is burnt, reacted Journey R50；

(6) the first high-temperature oxydation semicoke BS1 of R50 discharges enters riser pyrolytic reaction as the first solid thermal carriers R10KS The lower part of device R10E is mixed with fine coal；

(7) the second high-temperature oxydation semicoke BS2 of R50 discharges is used as the second solid thermal carriers SK2, and half is pyrolyzed with coming from containing for R10E Burnt material, before final pyrolysis char is formed Hybrid Heating it, the temperature of the second solid thermal carriers SK2, which is higher than, is mixed thing The temperature of material, the temperature of the second solid thermal carriers SK2 are less than the temperature of the first solid thermal carriers R10KS.

3. method and apparatus according to claim 2, it is characterised in that：

In system UNIT is burnt using the hydrocarbon powder R10FS of solid thermal carriers R10KS pyrolysis, in solid thermal carriers R10KS Circulate by workflow position, using the wind-force of gas-solid material carry out classification cyclonic separation and/or using fluidized wind to particle Semicoke particle carries out FLOTATION SEPARATION in bed, isolates under the critical grain size DZ in the material EM comprising solid thermal carriers at least A part of little particle LS, separation scheme use 1 or 2 or multiple in following：

2. scheme K02, is classified with gas cyclone in settler；

4. scheme K04, is classified with device flue gas cyclone separator is burnt；

5. scheme K05, is classified with gas cyclone in device is burnt；

4. method and apparatus according to claim 1, it is characterised in that：

The particle diameter of hydrocarbon powder R10FS is 0~6 millimeter, one or more of the hydrocarbon powder R10FS in following materials,：

1. low rotten fine coal；

2. high rotten fine coal；

3. oil shale powder；

4. oil-sand；

5. method and apparatus according to claim 5, it is characterised in that：

The particle diameter of hydrocarbon powder R10FS is 0~2 millimeter.

6. according to claim 1 or 2 or 3 or 4 or 5 the methods and equipment, it is characterised in that：

Critical grain size DZ numerical value in material EM comprising solid thermal carriers, uses 1 in following：

1. DZ≤5 micron；

2. DZ≤1 micron；

3. DZ≤0.5 micron；

4. DZ≤0.1 micron.

7. method and apparatus according to claim 2, it is characterised in that：

(1) in level-one pyrolytic reaction process R10, gas feed R10FV provides fluidisation power, level-one pyrolytic reaction process R10's At least most of caloric receptivity is provided by the first solid thermal carriers R10KS；

(4) in gas solid separation process S20, the pyrolysis coal gas of the dust-laden two level after solid powder main body bed is left, by least making Gas solid separation, gained dedirt two level pyrolysis coal gas are completed with the gas solid separation system S2 of the cyclone separator of 2 grades of serial operations R20PV is discharged from two level pyrolytic reaction process R20 reaction compartments top, and S20 and S10 is at least partly shared.

8. method and apparatus according to claim 2, it is characterised in that：

(3) it is empty in two level pyrolytic reaction process R20, the reaction of level-one pyrolysis char R10PS into two level pyrolytic reaction process R20 Between, main body flow direction is to flow from above to below, and level-one pyrolysis char R10PS carries out the second pyrolytic reaction R20R and produces two level pyrolyzing coal Gas and two level solution pyrolysis char, and complete gas solid separation；The Gas-particle Flows status and appearance of two level pyrolytic reaction process R20 is to dissipate formula Fluid bed.

9. method and apparatus according to claim 3, it is characterised in that：

Collecting tank LS-1W collects little particle LS in settler, and the lower part of collecting tank LS-1W, is passed through gas stripping gas LS-1V in settler With the tar gas and coal gas carried in air lift semicoke particle, gas stripping gas, which flows up, eventually enters into dedirt two level pyrolysis coal gas In R20PV.

10. method and apparatus according to claim 2, it is characterised in that：

(3) in the lower part of the two level pyrolytic reaction process R20 two level pyrolysis reactor R20E used, gas stripping gas V22V is passed through with gas The tar gas and coal gas carried in semicoke particle is carried, gas stripping gas, which flows up, to be eventually entered into dedirt two level pyrolysis coal gas R20PV.

11. according to 9 or 10 the method for claim and equipment, it is characterised in that：

Gas stripping gas, selected from coal gas or nitrogen and/or vapor and/or anaerobic flue gas.

12. method and apparatus according to claim 2, it is characterised in that：

(5) reaction process R50 is burnt in fluidisation, the final pyrolysis char RCPS based on two level pyrolysis char R20PS enters fluidisation Reaction compartment is burnt, is contacted with the oxygen-containing gas flowed from bottom to top, fluid bed occurs and burns reaction R50R, produces high-temperature semi-coke R50PS and flue gas YQ, flue gas YQ burn reaction process R50 from upper space discharge fluidisation；High-temperature semi-coke R50PS discharge fluidisations are burnt Burnt reaction process R50.

13. according to claim 12 the method and equipment, it is characterised in that：

(5) reaction process R50 is burnt in fluidisation, fluidizes ash-laden gas R50E- in the device for the top dilute phase section for burning reaction compartment YQ, the cyclone separation system S5 dedirts for the upper space for burning inside reactor by being arranged in fluidisation are separated into flue gas YQ and half Coke powder dirt R50-RS；Flue gas YQ leaves cyclone separation system S5 discharges fluidisation from upper space and burns reaction process R50.

14. according to claim 12 the method and equipment, it is characterised in that：

(5) reaction process R30 is burnt in fluidisation, fluidizes ash-laden gas R50E- in the device for the top dilute phase section for burning reaction compartment YQ, the cyclone separation system S5 dedirts for the upper space for burning inside reactor by being arranged in fluidisation are separated into flue gas YQ and half Coke powder dirt R50-RS；The semicoke dust R50-RS of the cyclone dip-leg discharge of cyclone separation system S5 returns to fluidisation and burns instead Space cycle is answered to process.

15. according to claim 12 the method and equipment, it is characterised in that：

(7) reaction process R50 is burnt in fluidisation, external warmer R50-OUT-HX is set, discharge fluidisation burns reaction process R50's After hot semicoke enters external warmer R50-OUT-HX and takes thermal medium indirect heat exchange to reduce temperature, external warmer R30-OUT- is discharged HX, cooling step XH is completed in heat collector R50-OUT-HX.

16. according to claim 12 the method and equipment, it is characterised in that：

(7) reaction process R50 is burnt in fluidisation, external warmer R50-OUT-HX is set, carrys out self-fluidized type and burns reaction process R50's Hot semicoke enters external warmer R50-OUT-HX and takes thermal medium indirect heat exchange to reduce temperature, discharge external warmer R50-OUT-HX The hot semicoke of at least a portion return to fluidisation and burn reaction process R50 recyclings, the hot semicoke of remainder is used as hot product R50PS-T, cooling step XH is completed in heat collector R50-OUT-HX.

17. according to claim 12 the method and equipment, it is characterised in that：

(7) reaction process R50 is burnt in fluidisation, external warmer R50-OUT-HX is set, carrys out self-fluidized type and burns reaction process R50's Hot semicoke enters external warmer R50-OUT-HX and takes thermal medium indirect heat exchange to reduce temperature, discharge external warmer R50-OUT-HX The hot semicoke of Part I return to fluidisation and burn reaction process R50 recyclings, be used as product R50PS- after Part II cooling C, cooling step XH is completed in heat collector R50-OUT-HX.

18. method and apparatus according to claim 2, it is characterised in that：

(3) in two level pyrolytic reaction process R20, two level pyrolysis reactor is also settler at the same time.

19. method and apparatus according to claim 2, it is characterised in that：

(1) in level-one pyrolytic reaction process R10, the particle diameter of hydrocarbon powder R10FS is 0~6 millimeter, and hydrocarbon powder R10FS is selected from The low rotten fine coal of high volatile；

The tar yield of level-one pyrolytic reaction process R10 is R10PY, the tar yield of two level pyrolytic reaction process R2 is R20PY With defining KR=R20PY/ (R10PY+R10PY), KR is 0.05~0.50.

20. method and apparatus according to claim 2, it is characterised in that：

(1) in level-one pyrolytic reaction process R10, the particle diameter of hydrocarbon powder R10FS is 0~6 millimeter, and hydrocarbon powder CHLS is selected from height The low rotten fine coal of volatile matter；

KR is 0.05~0.30.

21. method and apparatus according to claim 2, it is characterised in that：

Level-one pyrolytic reaction process R10, using riser fluidized bed pyrolysis reactor, the first solid thermal carriers R10KS be from Fluidisation burns the high-temperature oxydation semicoke of reaction process R50；

The operating condition of level-one pyrolytic reaction process R10 is：0.1~10s of reaction time, riser reacting product outlet temperature are Level-one pyrolytic reaction process cessation reaction temperature is 400~500 DEG C；

(3) in the reaction compartment of two level pyrolytic reaction process R20,2~12 secondary herringbone baffles or ring baffle, two level pyrolysis are set The temperature of the main pyrolysis section of reaction process is 460~700 DEG C；

Two level pyrolysis section bottom is passed through 450~650 DEG C of gas stripping gas V22V and carries out tar steam stripping, and gas stripping gas V22V passes through semicoke Flow up after the bed of material and be pyrolyzed into the two level of two level pyrolytic reaction process R20 in coal gas product；

Weight and fine coal R10FS weight ratios into the second solid thermal carriers SK2 of two level pyrolytic reaction process R20 are 0.3 ~10；

(4) in the gas solid separation process S20 of second level pyrolytic reaction gas-solid product, two level pyrolysis coal gas product is by thick rotation and top All gaps between rotation enter top whiz and open two level pyrolytic reaction space, in top medial rotation and the first pyrolytic reaction gas-phase product i.e. first Pyrolysis coal gas is mixed into row gas solid separation.

22. method and apparatus according to claim 2, it is characterised in that：

The operating condition of level-one pyrolytic reaction process R10 is：1.0~6s of reaction time, riser reacting product outlet temperature are Level-one pyrolytic reaction process cessation reaction is 430~470 DEG C；

(2) solids content is less than 10 grams/cube in gas-solid gas solid separation process S10, dedirt level-one pyrolysis coal gas R10PV Rice；

(3) in the reaction compartment of two level pyrolytic reaction process R20,2~12 secondary herringbone baffles or ring baffle, two level pyrolysis are set The temperature of the main pyrolysis section of reaction process is 480~600 DEG C；

Weight and fine coal R10FS weight ratios into the second solid thermal carriers SK2 of two level pyrolytic reaction process R20 are 1.0 ~5；

23. method and apparatus according to claim 2, it is characterised in that：

The operating condition of level-one pyrolytic reaction process R10 is：2.5~4s of reaction time, riser reacting product outlet temperature are Level-one pyrolytic reaction process cessation reaction is 440~460 DEG C；

(2) solids content is less than 4 grams/cubic metre in gas-solid gas solid separation process S10, dedirt level-one pyrolysis coal gas R10PV；

(3) in the reaction compartment of two level pyrolytic reaction process R20,2~12 secondary herringbone baffles or ring baffle, two level pyrolysis are set The temperature of the main pyrolysis section of reaction process is 480~530 DEG C；

Into the second solid thermal carriers SK2 of two level pyrolytic reaction process R20 weight and fine coal R10FS weight ratios for 2~ 3；

24. method and apparatus according to claim 2, it is characterised in that：

The riser fluidized bed pyrolysis reactor R10E that level-one pyrolytic reaction process R10 is used, with two level pyrolytic reaction process R20 The two level fluidized bed pyrolysis reactor R20E composition unit equipments used.

25. method and apparatus according to claim 2, it is characterised in that：

The two level fluidized bed pyrolysis reactor R20E that two level pyrolytic reaction process R20 is used, burning reaction process R50 with fluidisation makes Fluid bed burns reaction process R50E composition unit equipments.

26. method and apparatus according to claim 2, it is characterised in that：

Riser fluidized bed pyrolysis reactor R10E, the two level pyrolytic reaction process R20 that level-one pyrolytic reaction process R10 is used make Two level fluidized bed pyrolysis reactor R20E, fluidisation burn the fluid bed that reaction process R50 is used and burn reaction process R50E, Form unit equipment.

27. method and apparatus according to claim 2, it is characterised in that：

The two level fluidized bed pyrolysis reactor R20E that two level pyrolytic reaction process R20 is used, fluidisation burn reaction process R50 uses Fluid bed to burn reaction process R50E be vertical equipment, from locus, absolute altitude is said, its mutual alignment relation is：Fluid bed Burn the final pyrolysis half that the bottom of reactor R50E is lower than the bottom of two level pyrolysis apparatus R20E, and two level pyrolysis apparatus R20E is discharged Jiao burns the bottom of reactor R50E by material position difference inflow fluid bed.

28. method and apparatus according to claim 2, it is characterised in that：

The two level fluidized bed pyrolysis reactor R20E that two level pyrolytic reaction process R20 is used, burning reaction process R50 with fluidisation makes Fluid bed burns reaction process R50E composition coaxial-type unit equipments；

It is coaxial-type Vertical Combination equipment that coaxial-type, which refers to that two level pyrolysis reactor R20E, fluid bed burn reactor R50E, Said from spatial relation, its mutual alignment relation is：Fluid bed surrounds two level with burning the space segment of reactor R50E The space of pyrolysis apparatus R20E；The pyrolysis char of bottom space from two level pyrolysis apparatus R20E flows into fluidisation by standpipe and plug valve Bed burns the lower space of reactor R50E.

29. method and apparatus according to claim 2, it is characterised in that：