CN108315044A

CN108315044A - The heat-carrying gas air flow bed gasification method and gasification burner of hydrocarbon material containing heavy hydrocarbon and/or solid

Info

Publication number: CN108315044A
Application number: CN201710063930.5A
Authority: CN
Inventors: 何巨堂
Original assignee: Individual
Current assignee: Luoyang Rui Hua New Energy Technology Development Co Ltd
Priority date: 2017-01-18
Filing date: 2017-01-18
Publication date: 2018-07-24

Abstract

The heat-carrying gas air flow bed gasification method and gasification burner of hydrocarbon material containing heavy hydrocarbon and/or solid, heavy hydrocarbon in recyclable direct hydrogenation liquefaction of coal raffinate VS；In gasification D1, gas heat carrier FG and VS, which is mixed into mixture V1P and sprays, forms air flow bed flash zone, particulate matter or hydrocarbon liquid fly along airflow field by injection kinetic energy and assemble after colliding gasification burner wall, heavy hydrocarbon vaporization enters in gas phase, 2 or multiple air flow beds intersect or collide the discrete velocity that the oil that can be improved in air-flow is expected admittedly, can arrange 2 grades or multi-stage countercurrent vaporescence；The rich solid hydrocarbon liquid of dedirt gas D1 PV condensations gained obtained by D1 can evaporate de- solid with FG mixing circulations；The pyrolysis coal gas obtained through fluid bed heat solution preocess AR10 after vaporization residue slag charge D1 PS discharge air flow bed vaporescence postcooling moldings or its molding mass dusting is used as FG secondary uses pyrolysis coal gas thermal energy and air lift function forms group technology；Blender and/or scraper can be arranged in slurry zone.

Description

The heat-carrying gas air flow bed gasification method and gasification burner of hydrocarbon material containing heavy hydrocarbon and/or solid

Technical field

The present invention relates to heat-carrying gas air flow bed gasification method and gasification burner containing heavy hydrocarbon and/or the hydrocarbon material of solid, recyclable coals Add heavy hydrocarbon in hydrogen direct liquefaction raffinate VS；It is mixed into mixture V1P in gasification D1, gas heat carrier FG and VS and sprays shape At air flow bed flash zone, particulate matter or hydrocarbon liquid flys along airflow field by injection kinetic energy and assemble after colliding gasification burner wall, weigh Hydrocarbon vaporization enters in gas phase, and 2 or multiple air flow beds intersect or collide the discrete velocity that the oil that can be improved in air-flow is expected admittedly, It can arrange 2 grades or multi-stage countercurrent vaporescence；The rich solid hydrocarbon liquid of dedirt gas D1-PV condensations gained can be with FG mixing circulations obtained by D1 Evaporation is de- solid；Through fluidisation after the remaining slag charge D1-PS discharges air flow bed vaporescence postcooling molding of vaporization or its molding mass dusting The pyrolysis coal gas that bed pyrolytic process AR10 is obtained is used as FG secondary uses pyrolysis coal gas thermal energy and air lift function forms group technology； Blender and/or scraper can be arranged in slurry zone.

Background technology

Below by taking direct hydrogenation liquefaction of coal generates the recycling of the tower bottoms VS of the vacuum fractionation tower of oil as an example, discuss The present invention.

Tower bottoms VS usually contains 40~65% organic matter such as oil, asphaltene, preasphaltene, is evaporated containing overweight Point such as hydro carbons of the normal boiling point higher than 600~630 DEG C, heavy distillat such as normal boiling point between 530~640 DEG C hydro carbons, in Matter fraction such as normal boiling point is between 430~530 DEG C of hydro carbons, and rich in condensed-nuclei aromatics such as asphaltene, preasphaltenes.

Currently, coal liquefaction residue trans-utilization there is no suitable commercial technologies, the research of trans-utilization mainly to concentrate It is pyrolyzed in burning, gasification, extraction, hydro-conversion approach and directly：

1. burn approach, just with the combustion heat of its contained combustible component (mainly carbon, protium), to therein The liquid hydrocarbon structure such as oil, asphaltene, preasphaltene forms Oxidative demage, forms and greatly wastes, and briefly, reduces Coal liquefaction oil product weight yield is up to 10~16%, and waste is surprising；The products molecule structure feature of its carbon hydrogen element is all Low boiling point small molecule CO, CO₂、H₂O etc. realizes that component chemical Reaction Separation converts solid-liquor separation process to " burning+flue gas It is detached with slag "；

2. gasify approach, just with its contained gasifiable component (mainly carbon, protium), equally to oil therein, The liquid hydrocarbon structure such as asphaltene, preasphaltene forms Oxidative demage, and its essence is heavy oil gasifications, form and greatly waste, Briefly, it reduces coal liquefaction oil product weight yield and is up to 10~16%, waste is surprising；The products molecule knot of its carbon hydrogen element Structure is characterized in all low boiling point small molecules CO, CO₂、H₂、H₂O etc. realizes that component chemical Reaction Separation converts solid-liquor separation For " gasification+gasification gas is detached with slag "；

3. extraction routes, since the larger solid physics degree of isolation of the attraction between coal liquefaction residue molecule is too low, in this way Extraction routes certainly will be using the multiple extraction of the incremental multi-solvents of low-boiling armaticity of high agent-oil ratio, therefore, flow Complexity invests big, high energy consumption, and economy is very poor；Extraction routes do not break away from solid-liquor separation thinking substantially, it is unfavorable the result is that Inevitable；The products molecule structure feature of its carbon hydrogen element is to retain original molecule structure, realizes component separation；

4. hydro-conversion approach belongs in fact, this process is inherently included in DCL/Direct coal liquefaction hydrogenation process In the circulation liquefaction process of cycle residue, while partial catalyst is recycled, but forms catalysis in reactor in order to prevent Agent, the accumulation of non-fluidized solid, it is necessary to dead catalyst, non-fluidized solid be discharged, and at the same time carried oil, asphaltene secretly；Thing In reality, if it is possible to detach " oil, asphaltene, preasphaltene " with " insoluble matter, semicoke, ash content ", these are " oil, asphaltene, preceding Asphaltene " can be recovered；The products molecule structure feature of its carbon hydrogen element is to increase protium to realize lighting, realizes component Chemical reaction separation, but actual conversion is very low, and the behaviour of severe exacerbation Coal liquefaction process and product separation process Make condition, increase material quantity；

5. directly pyrolysis or coking processing, for producing tar, semicoke and coal gas, either autoclave coking, delayed coking, Fluid coking promotes which kind of mode such as tubular type pyrolysis, and since the operating time of pyrolysis or coking processing procedure is too long, (such as autoclave is burnt Change, delayed coking) or operation temperature it is too high (such as fluid coking, promoted tubular type pyrolysis up to 520~650 DEG C it is even higher), because This causes wide variety of conventional boiling point that thermal condensation reaction occurs between 530~660 DEG C of hydro carbons to generate a large amount of coke, hydrocarbon ils recycling compared with It is low.

It should be strongly noted that direct hydrogenation liquefaction of coal generates the tower bottoms VS of the vacuum fractionation tower of oil, containing big The condensation aromatic ring material of amount asphaltene, this high value for possessing special molecular structure of preasphaltene, if extraction obtains these Asphaltene, preasphaltene can go out the expensive high-end functionality carbon products such as carbon fiber by properly processing with final production, But at present since the limitation of technology can not recycle them.

In order to break away from the defect that aforementioned " burning, gasification, extraction, hydro-conversion approach and directly pyrolysis " all methods are constituted, It improves the yield of hydro carbons in tower bottoms VS and retains its molecular physics form as possible, especially for recycling asphaltene, preceding drip Green olefinic constituent must just avoid high temperature and/or prolonged operating condition, to inhibit green coke, chain-breaking reaction, the best way to be Air lift method is heated and/or depressurized using thermophilic and forms rapid physical flash distillation or vaporization, it is contemplated that the hydro carbons in tower bottoms VS is exhausted Major part belongs to hydro carbons of the normal boiling point higher than 530 DEG C and containing wide variety of conventional boiling point between 530~630 DEG C of hydro carbons, this hair It is bright to consider to realize that the combination vaporization mode of " quick heating+air lift depressurizes " carries out hydrocarbon and admittedly divides to tower bottoms VS using heat-carrying gas From concrete mode is the air flow bed flash evaporation that use can realize tower bottoms VS " discretization ", and passes through and increase particle External surface area strengthens straggling effect to strengthen heavy hydrocarbon vaporization.

Chinese patent application 201610028918.6 proposes to be extracted in the logistics of self-contained solid particle and heavy hydrocarbon a kind of The method of oil, is suitable for the process of oil-containing semicoke extract oil existing for direct hydrogenation liquefaction of coal process, and oily solid separation effect can be improved Rate；Belong to entropy increasing process this essence understanding based on oily solid separation, using in or beyond direct hydrogenation liquefaction of coal procedures system Boiling point is suitable, thermal stability is suitable, pressure is suitable logistics prepares gas heat carrier, using " the quick-fried cloud of fluid bed flashes " side Formula quickly transmits surface energy, thermal energy, kinetic energy to target material, realizes the discretization of the solid of oil-containing semicoke, realizes that multidimensional increases entropy Effect.

Chinese patent application 201610028918.6, in order to inhibit the classification of conventional distil-lation technique to flash to greatest extent The effect of " light component flash distillation necessarily causes remaining liquid phase degree of reviewing to reduce ", shortens " flash process period ", most to greatest extent Limits form " quickly directly heat and rapid flash " integrated process, realize thermodynamics space minimization " single-stage is theoretical Flash distillation ", using gas obtained by the flash of steam of the low boiling component inside semicoke particle as purge gas, " from inside to outside " punching The hydrocarbon ils liquid phase especially high boiling hydrocarbon fluid phase in semicoke duct is hit, the " quick-fried to blow effect of naphtha steam blowout heavy oil liquid is formed Answer ", " quick-fried cloud thermal shock flash distillation " is formed, two steps of cloud and thermal shock is dispersed into order to strengthen, two-way heat-carrying gas may be used Or heat-carrying qi leel is executed into dispersion, heating tasks respectively for two-way, quick-fried cloud thermal shock flash distillation is decomposed into 2 or multiple series connection steps It carries out, such as " quick-fried cloud+thermal shock flash distillation ", " quick-fried cloud+thermal shock+flash distillation ", " quick-fried cloud+thermal shock+flash distillation+gas solid separation ", very It can extremely be formed multistage " quick-fried cloud flash distillation ".

Chinese patent application 201610028918.6, technological deficiency be, the range of choice of the heat-carrying gas KTEG used It is limited, mostly come from that boiling point in or beyond direct hydrogenation liquefaction of coal procedures system is suitable, thermal stability is suitable, pressure is suitable Logistics prepares gas heat carrier, and heat-carrying gas KTEG is mainly made of hydrocarbon vapours, the limitation due to thermal cracking of hydrocarbons temperature in this way, The operation temperature of heat-carrying gas KTEG can not possibly be too high, therefore causes heat-carrying gas flow rate huge, certainly will form huge hydrocarbon material in this way Cycle causes fractionating column system scale to increase severely, increases a large amount of energy consumption and construction investment.Clearly, if it is possible to which searching out can With the bulk gas for forming suitable (heavy hydrocarbon gaseous phase partial pressure is low) of the secondary suitable temperature (approaching pyrolysis temperature lower limiting value) used Heat-carrying gas KTEG is served as, the economy of operating process will be increased substantially, bring huge economic benefit.And hydrocarbon powder such as powder The riser heat that coal, oil solid powder pyrolytic process such as CN105602593A, CN105694933A method and its improved method carry out The pyrolyzing coal divided containing a small amount of semicoke particle, low oil gas that the temperature for solving substantial amounts present in product is 450~530 DEG C Gas, for the present invention provides selectable heat-carrying gas KTEG.

CN105602593A, CN105694933A method and its improved method, basic principle can be regarded as certain By petroleum industry wax oil or the graft application of the reaction-regeneration system technology in the fluidized catalytic cracking field of residual oil in degree.In slag In the fluidized catalytic cracking reaction-regeneration system of oil, one way by raw material be the residual oil of atomization, its product be gaseous breakdown The material of oil gas, cyclic process is powdery solid catalyst, and the catalyst of discharge riser catalytic thermal cracker is coking Rear catalyst solid, coking rear catalyst complete degassing, subsequently into making charcoal by the cyclone separation system arranged in settler Device or regenerator carry out coke-burning regeneration, and the regenerated catalyst powder of high temperature state is returned as solid thermal carriers and catalyst to be promoted It is fluidized catalytic cracking anti-to be mixed progress under lift gas effect with the residual oil of atomization for the lower entrances of pipe reactor It answers, hot catalyst carries after at least part heat that regenerator generates is returned the regeneration of riser catalytic thermal cracker Enter the heat source that riser catalytic thermal cracker serves as thermal cracking process.The fluidized catalytic cracking reaction regeneration system of residual oil System, has had more than 50 years successful operating history, enlargement monosystem array apparatus process residual oils amount up to 400~8,000,000 tons/ Year, catalyst circulation amount up to 2000~40,000,000 tons/year i.e. 2500~5000 tons/when.With wax oil or residual oil fluidized catalytic The reaction-regeneration system of cracking is compared, CN105602593A, CN105694933A method, using similar riser reactor into Row pulverized coal pyrolysis reacts, and the gas of pulverized coal pyrolysis reaction product is completed using similar cyclone separation system (being arranged in settler) Gu separation carries out coke breeze combustion with meagre oxygen using similar device of making charcoal, a part for the hot semicoke that device of making charcoal generates is as solid thermal Carrier enters riser reactor to the heat supply of pyrolysis of coal reaction process and forms the circulatory system, extra semicoke discharge system and/or Oxidizing fire discharges heat.

In the system described in CN105602593A, CN105694933A, one way by raw material be fresh solid fine coal, Pyrolysis product is gaseous state coal gas and solid semicoke, the material of cyclic process be solid semicoke (semicoke product of pyrolytic reaction or Semicoke cycle stock), the solid oxidation semicoke of high temperature state returns to the lower entrances of riser reactor as solid thermal carriers, is carrying It rises under gas effect, is mixed with fresh coal dust and carries out fluidization pyrolytic reaction.Two kinds of technologies are can be seen that from above-mentioned comparison Pyrolysis reactor, thermal decomposition product gas solid separation system, pyrolysis solid product settler, solid circle material make charcoal device, it is identical The type of flow of the gas-solid fluid of workflow position is essentially identical.Due to the above-mentioned similitude of the two, CN105602593A, CN105694933A methods greatly simplifie system structurally and operationally, greatly improve the safety of system, are deep tools The technical method of large industrialized potentiality.

It is proposed the premise of " the heat-carrying gas air flow bed gasification method and gasification burner of the hydrocarbon material containing heavy hydrocarbon and/or solid " of the invention, It is to be had the characteristics that based on tower bottoms VS：

1. the semicoke solid for giving full play to liquefaction raffinate VS belongs to the bulk cargo of fine particle, and has Coal liquefaction mistake Journey is formed a large amount of to outward opening inner duct, and based on having to outward opening inner duct, wherein Medium Diffusion resistance is small or outside injection The small feature of resistance can form quick " open type vaporization ", " open type pyrolysis "；

2. hydrocarbon material FS01, sprayed after mix with the material FG (preferably heat-carrying gas FG) containing gas formed air flow bed i.e. by Start discretization in impact；In air flow bed, with the further discretizations of vaporised hydrocarbon material FS01 of hydro carbons between particle, to increase The external surface area of particle further promotes the vaporization of the discrete and hydro carbons of solid particle；

3. the solid particle in hydrocarbon material FS01 substantially belongs to solid granule, but forms one under the bonding of heavy hydrocarbon The ratio of external surface area/volume of the aggregation JJS of fixed number amount solid particle, aggregation JJS is much smaller than single solid particle The ratio of external surface area/volume, the flow behavior of aggregation JJS have been detached from the feature of single solid particle；

In air flow bed, discretization may be implemented in hydrocarbon material FS01, and solid particle and the hydrocarbon liquid of carrying are generated by kinetic energy Opposite directed movement (orientation flight is splashed), assembles after colliding gasification burner wall；It can make to splash in gasification burner along gravitational field Congregate；

In a first aspect, using gas obtained by the flash of steam of the low boiling component in semicoke particle internal gutter as semicoke The hydrocarbon ils liquid phase especially high boiling hydrocarbon fluid in semicoke duct is impacted in " built-in " purge gas of internal gutter, " from inside to outside " Phase can form " quick-fried to blow effect " of naphtha steam blowout heavy oil liquid, be detached from semicoke particle and enter gas phase or other particle appearances The high boiling hydrocarbon oil drops in face are because of the state of aggregation liquid phase environment condition that the suction-operated for having broken away from the surface of solids is formed, in gas phase In become the free small particle high surface area liquid particle in low oil gas gaseous phase partial pressure, can be real more quickly to a greater degree It now vaporizes and enters in gas phase, gas solid separation is completed, to give full play to " Moderate High Temperature, enormous quantity, the low heavy hydrocarbon of heat-carrying gas Oil gas partial pressure, operation stagnation pressure are relatively low " many advantages, such as；The present invention substantially contains one " in particle inner duct from inside to outside Flash distillation quick-fried blow over journey "；

Second aspect, a large amount of sensible heats that hydrocarbon powder pyrolysis coal gas carries need secondary efficient utilization, but due to pyrolysis The high boiling hydrocarbon such as colloid, asphalitine that coal gas carries semicoke particle simultaneously and easily condensation deposits, are recycled using indirect heat exchanger Necessarily cause the quick fouling of heat transfer interface that heat-transfer capability is made to decline when thermal energy, due to being difficult to indirect heat exchange, these heats usually quilt Compel to be converted into the lower thermal energy of temperature；And in the present invention, the thermal energy of these higher temperatures can obtain almost most direct profit With, using subtract tower bottoms VS be heat-recovery medium directly absorb heat, thermal energy organic efficiency is high；The present invention substantially includes One " the direct transmission of high temperature heat " process；

The third aspect, for component separating step, semicoke particle and the height boiling for easily condensing deposition that pyrolysis coal gas carries Point hydrocarbon such as colloid, asphalitine, preferably detach abjection, utmostly to reduce semicoke particle in first separating step from gas phase The high boiling hydrocarbon flow range as existing for colloid, asphalitine deposited with easy condensation, therefore it is de- by a condensation to be pyrolyzed coal gas Heavy hydrocarbon, de- solid step, are suitable；The present invention substantially contains one, and " the heavy hydrocarbon component rectifying in similar destilling tower is cold It is solidifying " process；

Fourth aspect consolidates entropy variable analysis from process liquid, and pyrolysis coal gas is isolated in first separating step from gas phase Remaining slag after the high boiling hydrocarbon such as colloid, asphalitine of the semicoke particle of carrying and easily condensation deposition, with tower bottoms VS vaporizations Particulate matter and the hydrocarbon composition of material, the two are close or identical, and marker method, post-production technique are also highly consistent, use pyrolysis Coal gas carries out tower bottoms VS mixing and the energy redistribution process that air flow bed evaporation process is same or similar component, and Do not cause other unnecessary " detaching task again ", integrating mixed process does not have to generate new " extra phase ", does not generate volume Outer " entropy production "；The present invention substantially contains " the entropy flow merging of a similar heavy hydrocarbon, solid component " process；

5th aspect, the solid-liquid entropy variable analysis from process gas phase are pyrolyzed the height boiling of the easy condensation deposition carried in coal gas Point hydrocarbon such as colloid, asphalitine, once as being to be pyrolyzed semicoke particle aggregation in coal gas into the binder of bulky grain or poly- if droplet Collection center, at the same the tower bottoms VS containing high viscosity heavy oil of enormous amount be also pyrolysis coal gas in semicoke particle aggregation at big The binder of grain, the two are conducive to fine ash, the reunion of fine ash shape semicoke particle and disengaging gas phase, therefore, the present invention or one kind " solid subtracts entropy in gas phase " technique；

6th aspect removes angle analysis from flying dust, and the shell ring aggregation oil droplet in pleasant flow field can be arranged or contain solid oil droplet, Then continuously removed, collect, be discharged with mechanical scraper machine, this be equivalent to provided with it is online, replaceable, can continuously give birth to automatically The malthoid filtration system of long absorption fine particulates, therefore, the present invention also constitute a kind of " spontaneous formula malthoid adheres to particle " Technique；

7th aspect is separated into the angle that the remaining slag charge D1-PS of vaporization is used as fluidized bed pyrolysis raw material from liquefaction raffinate VS Analysis, with liquefaction raffinate VS be used as fluidized bed pyrolysis raw material scheme compared with, in fluidized bed pyrolysis raw material can vaporised hydrocarbon number Amount is greatly lowered, and therefore, can reduce pyrolytic process raw material quantity, the quantity for reducing pyrolytic process solid thermal carriers, reduce Gas yield can effectively shorten stream at this point, present invention process effect is the heaviness for realizing fluid bed heat solution preocess raw material The time for changing initial stage temperature-rise period of the bed pyrolysis feed in riser fluidized-bed reactor, reduce the liquefaction on solid material surface The particle agglomeration probability that heavy hydrocarbon induces reduces the necessary caloric receptivity of pyrolytic process, constitutes a kind of " direct hydrogenation liquefaction of coal generation The mixture of air flow bed light slag oil and gas+air flow bed heavy oil residue and solid of conventional distil-lation process+destilling tower base oil of oil Fluidized bed pyrolysis " group technology；

4. 2 or multiple air flow beds intersect or collide the discrete velocity that the oil that can be improved in air-flow is expected admittedly；

5. to the raffinate VS that liquefies, 2 grades or Multi-stage airflow bed evaporation process, preferably reverse-flow 2 grades or multistage can be built Air flow bed evaporation process can add low boiling point or moderate boiling point in the oily Guyuan material of 2 grades or Multi-stage airflow bed evaporation process Hydrocarbon ils increases in the dispersibility, mobility, hole of the remaining slag charge of vaporization and evaporates hydro carbons quantity, effectively improves weight in liquefaction raffinate VS The evaporation rate of recovery of hydrocarbon；

6. the solid particle in hydrocarbon material FS01 substantially belongs to solid granule, but forms one under the bonding of heavy hydrocarbon The ratio of the aggregation JJS of fixed number amount solid particle, external surface area/volume of aggregation are much smaller than single solid particle, gas The action of draging of aggregation uses the action of draging of single solid particle with much smaller than gas, therefore, the JJS in gas phase is easily achieved Gas solid separation；

Bottom in vaporization gas stream in the stove field, air-flow can form steering flowing and form gas turns area V3, and gas phase turns to Flowing, can be obtained dedirt gas V3-PV, dedirt gas V3-PV can condensed mistake by the solid decanting zone of big runner low gas velocity Journey such as condensation fractionating column recycles hydrocarbon ils；

7. lower part slurry zone V4 can be used mechanical discharger such as auger stripper and draw off slurry V4-PS or solid-state material； V4-PS can be cooled and shaped；

Slurry zone, setting blender can crush oily solid material, and setting scraper can remove wall oil and expect admittedly online；

8. in fluid bed heat solution preocess AR10, through fluid bed heat solution preocess AR10 after slurry V4-PS or its molding mass dusting Obtained pyrolysis coal gas forms group technology as FG.

Based on the above analysis, basic imagination proposed by the present invention is：The present invention relates to the hydrocarbon material containing heavy hydrocarbon and/or solid Heat-carrying gas air flow bed gasification method and gasification burner, heavy hydrocarbon in recyclable direct hydrogenation liquefaction of coal raffinate VS；In gasification D1, gas Body heat carrier FG and VS, which is mixed into mixture V1P and sprays, forms air flow bed flash zone, and solid is by injection kinetic energy along airflow field It flies and assembles after colliding gasification burner wall, heavy hydrocarbon vaporization enters in gas phase, and 2 or multiple air flow beds intersect or collide can The discrete velocity that the oil in air-flow is expected admittedly is improved, 2 grades or multi-stage countercurrent vaporescence can be arranged；Dedirt gas D1-PV obtained by D1 The rich solid hydrocarbon liquid of condensation gained can evaporate de- solid with FG mixing circulations；After the remaining slag charge D1-PS discharges air flow bed vaporescence of vaporization The pyrolysis coal gas obtained through fluid bed heat solution preocess AR10 after cooling and shaping or its molding mass dusting is pyrolyzed as FG secondary uses Coal gas thermal energy and air lift function form group technology；Blender and/or scraper can be arranged in slurry zone.

The heat-carrying gas air flow bed gasification method and gasification burner of hydrocarbon material of the present invention containing heavy hydrocarbon and/or solid, can be handled similar In the various materials of direct hydrogenation liquefaction of coal raffinate VS, coal tar, coal tar asphalt, such as following materials：

1. direct hydrogenation liquefaction of coal generates the tower bottoms of the vacuum fractionation tower of oil；

2. heavy oil floating bed hydrogenation generates the tower bottoms of the vacuum fractionation tower of oil；

3. the heavy oil discharge material of coal tar oil eliminator；

4. the heavy oil discharge material of the condensation fractionator of pulverized coal pyrolysis coal gas；

5. oil-sand is pyrolyzed the heavy oil discharge material of the condensation fractionator of coal gas；

6. shale oil is pyrolyzed the heavy oil discharge material of the condensation fractionator of coal gas；

7. material is discharged in the bottom oil containing solid heavy oil evaporator admittedly；

8. other solid material of oil；

9. other heavy oil material.

The recycling of liquefaction raffinate VS, the present invention, being belonged to based on raffinate " can evaporate heavy hydrocarbon+superelevation boiling point high viscosity heavy hydrocarbon+richness This essence of the bulk cargo solid particle in the internal control road containing opening " thus separation characteristic with " be easy to be vaporized and discretization " is recognized Know, fundamentally changes the recovery technology path of heavy hydrocarbon in existing tower bottoms VS, have the following advantages that：

1. using the evaporation mode of physics, the hydro carbons of recycling maintains original molecular structure substantially, it is suppressed that heaviness Reaction, therefore hydrocarbon recovery is high；

Especially it is possible to the condensation of this high value for possessing special molecular structure of recovery section asphaltene, preasphaltene Aromatic ring material；Asphaltene, preasphaltene can go out the high-end carbon material such as carbon fiber by suitable processing with final production；

2. the thermal energy of the higher temperatures position using high temperature or hot hydrocarbon material FS01 itself, being especially directly utilized can evaporate The existing thermal energy of hydrocarbon reduces procedure of processing to reduce energy consumption；

3. tower bottoms VS is separated into vaporization heavy hydrocarbon and " superelevation boiling point high viscosity heavy hydrocarbon+bulk cargo solid through the present invention The remaining slag charge D1-PS of grain " vaporization, vaporizes the softening point higher of hydro carbons in remaining slag charge D1-PS, and vaporizes remaining slag charge D1- The heavy hydrocarbon liquid on the surfaces PS can flow under the capillarity in solid duct from trend duct, to improve solid particle Dispersion, therefore vaporization residue slag charge D1-PS is more easily drawn off and curing molding；

4. the pyrolysis that vaporization residue slag charge D1-PS or its molding mass atomized particles material are obtained through fluid bed heat solution preocess AR10 Coal gas is typically that de- solid coal gas forms group technology as FG；In this way to tower bottoms VS, constitute " air flow bed evaporation+ The fluidized bed pyrolysis of air flow bed residue " group technology；This is also the rational flow arrangement of nature；

In air flow bed gasification burner, the super high boiling tar condensing in part in coal gas simultaneously enters the remaining slag charge of vaporization In D1-PS, the part to also achieve coal gas takes off heavy hydrocarbon task；

Also, due in the remaining slag charge D1-PS of vaporization Volatile Hydrocarbons or volatile matter be far below tower bottoms VS, because This can reduce fluidisation compared with directly by " the fluid bed heat solution preocess of tower bottoms VS or its molding mass atomized particles material " Bed pyrolytic process raw material volatile matter content, therefore can reduce pyrolytic process heating load thus solid thermal carriers can be reduced In short the scale of fluid bed heat solution preocess can be greatly lowered, to reduce investment and energy consumption in quantity；

5. the pyrolysis that vaporization residue slag charge D1-PS or its molding mass atomized particles material are obtained through fluid bed heat solution preocess AR10 Some or all of coal gas, typically de- solid coal gas are used as FG, constitute " the fluid bed of air flow bed evaporation+air flow bed residue Pyrolysis " group technology, wherein with air flow bed evaporation process recycled " fluidized bed pyrolysis of air flow bed residue " generation containing tar, The sensible heat of coal gas of high temperature containing solid particle, and the sensible heat of such coal gas is difficult to recycle using conventional method, phase of the present invention When in the heat recovery for realizing direct heat transfer formula, therefore, for tower bottoms VS, air flow bed gasification burner is a name Fu Qi The gasification burner of heavy hydrocarbon in real raffinate VS, for being pyrolyzed coal gas, air flow bed gasification burner is a pyrolysis coal gas worthy of the name Sensible heat recovery furnace；

6. the body containing solid and gas being discharged after air flow bed evaporation, it is such as conventional to be separated into ultraheavy fraction into condensation separation process Boiling point higher than 600~630 DEG C hydro carbons, heavy distillat such as normal boiling point between 530~600 DEG C hydro carbons, middle matter fraction such as Normal boiling point between 430~530 DEG C hydro carbons, light fraction such as normal boiling point less than 450 DEG C hydro carbons, coal gas and water；Its In, the fraction rich in asphaltene, preasphaltene can be separately separated out；Wherein, the heavy distillat rich in solid particle isolated For example normal boiling point is between 530~600 DEG C of hydro carbons, it can be directly as the coal of direct hydrogenation liquefaction of coal reaction process Feedstock oil with slurry simultaneously eventually enters into direct hydrogenation liquefaction of coal reaction process；Wherein, that isolates evaporates rich in the overweight of solid particle Divide such as normal boiling point to be higher than 600~630 DEG C of hydro carbons, gasification burner cycle can be gone to be vaporized solid-liquor separation, can be cooled down Molding or its molding mass dusting be particulate material after can go fluid bed heat solution preocess go joint processing 2 kinds or plurality of raw materials fluidisation Bed pyrolytic process；

7. the structure type similar to water leg used by Lurgi gasifier may be used in air flow bed gasification burner, control The temperature of the accumulation regions of the remaining slag charge D1-PS of vaporization of the bottom of wall is in reduced levels, to inhibit the coking product of wall Amount is conducive to extend the operation cycle；

8. tower bottoms VS or vaporization residue slag charge D1-PS are cooled to moulding mixture, through forcing discharger that can become non-heap Buildup VS-MS；Non-stacking material VS-MS refers to that discharge material VS-MS has been forced removal device SK such as screw dischargers and has carried out A degree of " crushing " is also conducive to subsequent to carry out a degree of destruction to " the hardened property " of solid material therein It is cooled and shaped；The exhaust end of screw discharger can coordinate and arrange material cleaner such as a discharging version or discharging knife.

The solid mixture VS of oil of the present invention, hydro carbons therein is mainly by normal boiling point higher than 550 DEG C or higher than 580 DEG C The hydrocarbon component composition, softening point usually above 120 DEG C or be higher than 150 DEG C, the present invention, can recycle 530~630 DEG C of fractions or 530~600 DEG C of fractions, it is even more (to direct hydrogenation liquefaction of coal device feed coal weight) to can be improved distillate oil 6~8%, effect Fruit is huge.

Pervaporation step can be carried out with the subsequent job step of dedirt gas D1-PV in unit equipment；

Pervaporation step can be carried out with the condensation separation step of dedirt gas D1-PV in unit equipment；

Pervaporation step can be carried out with the subsequent job step of the remaining slag charge D1-PS of vaporization in unit equipment；

Pervaporation step can be carried out with the cooling and shaping step of the remaining slag charge D1-PS of vaporization in unit equipment；

It can be by the cooling and shaping device of non-stacking material VS-MS and pressure removal device SK being combined into one equipment.

It can be by the cooling and shaping device of non-stacking material VS-MS, pressure removal device SK and gasification burner being combined into one of HVD-F Equipment.

It can be by the cooling and shaping device of non-stacking material VS-MS, pressure removal device SK, gasification burner HVD-F and gas condensation point Evaporate tower being combined into one equipment.

As needed, suitable low boiling hydrocarbon can be mixed into the hydrocarbon material FS01 comprising hydrocarbon and granular solids, with enhancing Its mobility, dispersibility can also form the heavy hydrocarbon in hydrocarbon material FS01 extraction effect, be conducive to improve the recycling of vaporescence heavy hydrocarbon Rate.

The method of the invention has not been reported.

Therefore, an object of the present disclosure is to propose the heat-carrying gas air flow bed gasification method of the hydrocarbon material containing heavy hydrocarbon and/or solid And gasification burner.

Second purpose of the invention is to propose the heat-carrying gas air flow bed gasification method of the hydrocarbon material containing heavy hydrocarbon and/or solid and vapour Change stove, belongs to 2 grades or Multi-stage airflow bed evaporation process, preferably reverse-flow 2 grades or Multi-stage airflow bed evaporation process, 2 grades or more The hydrocarbon ils that low boiling point or moderate boiling point can be added in the oily Guyuan material of grade air flow bed evaporation process increases the remaining slag charge of vaporization Dispersibility, mobility evaporate hydro carbons quantity in hole, effectively improve the evaporation rate of recovery of heavy hydrocarbon in liquefaction raffinate VS.

Third purpose of the present invention is to propose the heat-carrying gas air flow bed gasification method of the hydrocarbon material containing heavy hydrocarbon and/or solid and vapour Change stove, the richness that air flow bed vaporescence gained dedirt gas D1-PV condensation separations obtain, which is consolidated after heavy hydrocarbon liquid stream can be mixed with FG, to be followed Ring evaporation is de- solid.

4th purpose of the invention is to propose the heat-carrying gas air flow bed gasification method of the hydrocarbon material containing heavy hydrocarbon and/or solid and vapour Change stove, hydrocarbon powder such as fine coal, oil solid powder pyrolytic process such as CN105602593A, CN105694933A method and its improvement side The temperature of substantial amounts present in the riser thermal decomposition product that method carries out is 450~530 DEG C and contains a small amount of semicoke particle, low The pyrolysis coal gas of oil gas partial pressure, serves as the gas heat carrier FG that the present invention needs, and secondary use is pyrolyzed coal gas thermal energy and air lift work( Can, it is 0.30~0.50MPa to form group technology pyrolytic process pressurized operation such as operating pressure, and spray is provided for air flow bed evaporation Penetrate power.

5th purpose of the invention is to propose the heat-carrying gas air flow bed gasification method of the hydrocarbon material containing heavy hydrocarbon and/or solid and vapour Change stove, vaporizes the pyrolysis obtained through fluid bed heat solution preocess AR10 after remaining slag charge D1-PS cooling and shaping or its molding mass dusting Coal gas is used as FG secondary uses pyrolysis coal gas thermal energy and air lift function forms integral combined process, vaporizes remaining slag charge D1-PS It is converted into semicoke, coal gas, tar in pyrolytic process, that is, realizes partial gasification and partial liquefaction, pyrolytic process pressurized operation ratio If operating pressure is 0.30~0.50MPa, injection power is provided for air flow bed evaporation.

6th purpose of the invention is to propose that the heat-carrying gas air flow bed gasification method of the hydrocarbonaceous batch mixing containing solid particle uses Various structures gasification burner.

Invention content

The heat-carrying gas air flow bed gasification method and gasification burner of hydrocarbon material of the present invention containing heavy hydrocarbon and/or solid, it is characterised in that packet Containing following steps：

(1) in air flow bed vaporescence D1, the hydrocarbon material FS01 containing heavy hydrocarbon and/or solid, after being mixed with the material FG containing gas The vaporization that air flow bed completes at least part hydrocarbon FS01-CHL is formed, it is remaining to be separated into the vaporization being mainly made of solid and hydrocarbon liquid Slag charge D1-PS and contain evaporation hydrocarbon FS01-CHL gas D1-PV；

Air flow bed vaporescence D1, including following work step, uses air flow bed gasification burner HVD-F：

1. in mixing step D1-1, hydrocarbon material FS01 and FG containing gas material is mixed into mixture V1P；

2. spray to form air flow bed in air flow bed pervaporation step D1-2, V1P, hydrocarbon liquid and/or solid from hydrocarbon material FS01 according to It flies along the flow field of air flow bed by injection kinetic energy and assembles after colliding gasification burner wall, at least partially from hydrocarbon material FS01's Heavy hydrocarbon vaporization enters in gas phase；

3. in gas solid separation step D1-3, the gas from air flow bed, which deviates from least part liquid and/or solid, becomes de- Dust and gas body D1-PV；

4. in extraction step D1-4, remaining slag charge D1-PS discharge air flow bed gasification burners HVD-F is vaporized.

The present invention, in general, (1) is walked using air flow bed gasification burner HVD-F in gas solid separation in air flow bed vaporescence D1 Rapid D1-3, the gas turns from air flow bed simultaneously deviate from least part liquid and/or solid as dedirt gas D1-PV.

The present invention, generally, (1) are contacted with the material FG containing gas and are completed in air flow bed vaporescence D1, hydrocarbon material FS01 The vaporization of few a part of liquid hydrocarbon FS01-CHL, be separated into the vaporization residue slag charge D1-PS being mainly made of solid and hydrocarbon liquid and Gas D1-PV containing evaporation hydrocarbon FS01-CHL；

In air flow bed vaporescence D1, using air flow bed gasification burner HVD-F, including following work step：

1. in mixing step D1-1, the hydrocarbon material FS01 and material FG containing gas is mixed into mixture V1P, the operation of material FG Temperature is higher than the operation temperature of hydrocarbon material FS01；

2. in air flow bed pervaporation step D1-2, V1P forms air flow bed, the liquid or dynamic with solid dependence from hydrocarbon material FS01 It can splash and assemble along the flow field of air flow bed；

In air flow bed, the liquid hydrocarbon FS01-CHL at least part hydrocarbon material FS01 is evaporated into gas phase, Ke Nengyou High boiling hydrocarbon of the part from the FG containing gas material enters in the remaining slag charge D1-PS of vaporization；

3. in gas turns step D1-3, gas turns carry out gas solid separation by solid settlement space, obtain dust-removing gas Body D1-PV；

The preferable mode of operation of the present invention is that (1) is in air flow bed vaporescence D1, hydrocarbon material FS01 and the material FG containing gas The vaporization of at least part liquid hydrocarbon FS01-CHL is completed in contact, is separated into the vaporization residue slag being mainly made of solid and hydrocarbon liquid Expect D1-PS and the gas D1-PV containing evaporation hydrocarbon FS01-CHL；

1. in mixing step D1-1, the hydrocarbon material FS01 and material FG containing gas is mixed into mixture V1P, the material containing gas The operation temperature of FG is higher than the operation temperature of hydrocarbon material FS01；

2. in air flow bed pervaporation step D1-2, downwards or obliquely, i.e., the main body initial flow direction for the air flow bed that V1P is formed is Downward motion of at least part along gravitational field is carried out, solid and liquid from hydrocarbon material FS01 are by kinetic energy along air flow bed Flow field carries out at least part along the downward motion of gravitational field and mutually assembles；

The present invention, (1) are hot logistics in air flow bed vaporescence D1, hydrocarbon material FS01, and hydrocarbon material FS01 can be selected from down The one or more of row material：

3. the heavy oil discharge material of coal tar oil eliminator；

8. other solid material of oil；

9. other heavy oil material.

The present invention, (1) are hot logistics in air flow bed vaporescence D1, hydrocarbon material FS01, and temperature is usually 200~500 DEG C, generally 300~450 DEG C, common person be 350~400 DEG C.

The present invention, in general, (1) contains the liquid that weight concentration is 10~90% in air flow bed vaporescence D1, hydrocarbon material FS01 Body hydrocarbon, wherein being less than 650 DEG C of liquid hydrocarbons containing the normal boiling point that weight concentration is 3~40%.

The present invention, generally, (1) contain the liquid that weight concentration is 10~90% in air flow bed vaporescence D1, hydrocarbon material FS01 Body hydrocarbon, wherein being less than 650 DEG C of liquid hydrocarbons containing the normal boiling point that weight concentration is 5~30%.

The present invention, common person, it is 10~90% that (1) contains weight concentration in air flow bed vaporescence D1, hydrocarbon material FS01 Liquid hydrocarbon, wherein being less than 650 DEG C of liquid hydrocarbons containing the normal boiling point that weight concentration is 8~20%.

The present invention, in general, the diameter of the most of solid particle of (1) in air flow bed vaporescence D1, hydrocarbon material FS01 is small In 100 microns.

The present invention, generally, the diameter of the most of solid particle of (1) in air flow bed vaporescence D1, hydrocarbon material FS01 are small In 50 microns.

The present invention, common person, the diameter of the most of solid particle of (1) in air flow bed vaporescence D1, hydrocarbon material FS01 Less than 10 microns.

The present invention, (1) use air flow bed gasification burner HVD-F in air flow bed vaporescence D1；

1. in mixing step D1-1, hydrocarbon material FS01 and FG containing gas material is mixed into mixture V1P, and hydrocarbon material FS01 can divide For 1 or 2 or multiple branches, FG containing gas material can be divided into 1 or 2 or multiple branches, can form 1 or 2 Or multiple mixture branches being mixed by hydrocarbon material FS01 branches and the branches of FG containing gas material；

2 or multiple airflow fields can intersect or liquidate and entrained oil in air-flow is made to expect to collide admittedly.

The present invention, the temperature of (1) in air flow bed vaporescence D1, the FG containing gas material：Usually 400~600 DEG C, it is general To be 480~530 DEG C for 450~550 DEG C, common person.

The present invention, (1) in air flow bed vaporescence D1, the hydrocarbon material FS01 containing heavy hydrocarbon and/or solid normal boiling point between The vaporization rate of 530~630 DEG C of hydro carbons：Typically larger than 40%, it is generally higher than 60%, more preferably greater than 85%.

2. the air flow bed along gravitational field, the solid from hydrocarbon material FS01 can be formed in air flow bed pervaporation step D1-2, V1P It splashes along the flow field of air flow bed by kinetic energy with liquid and is gathered in the lower part of air flow bed gasification burner HVD-F.

In the solid settlement space, the tower tray for being disposed with duct can be set, to upward flowing air progress rectification and uniformly Distribution.

The present invention, further, (1) use air flow bed gasification burner HVD-F in air flow bed vaporescence D1；

4. in extraction step D1-4, vaporizing the mode of remaining slag charge D1-PS discharge air flow bed gasification burners HVD-F can be： Force removal device SK that will vaporize remaining slag charge D1-PS discharge air flow bed gasification burner HVD-F as non-stacking discharge using mechanical Expect D1-PS-MS；

D1-PS-MS is expected in the non-stacking discharge, refers to that discharge material D1-PS-MS has been forced removal device SK and has carried out A degree of " crushing " to " the hardened property " of solid material therein so that carried out a degree of destruction.

3. in gas turns step D1-3, gas carries out gas solid separation and obtains dedirt gas D1-PV；

Dedirt gas D1-PV can remove condensation fractional distillation process recycling hydrocarbon ils.

The present invention, further, (1) uses air flow bed gasification burner HVD-F in air flow bed vaporescence D1；

3. in gas turns step D1-3, isolated dedirt gas D1-PV is consolidated in the promoting the circulation of qi of going forward side by side of gas reduction of speed；

Dedirt gas D1-PV, can go condensation fractional distillation process recycling hydrocarbon ils, recycling obtain mainly by normal boiling point between The heavy distillat rich in asphaltene, preasphaltene of 530~630 DEG C of hydro carbons composition, heavy distillat are used as preparing the raw material of carbon fiber.

Dedirt gas D1-PV, removes condensation fractional distillation process recycling hydrocarbon ils, recycling obtain mainly by normal boiling point between 530~ The heavy distillat of 630 DEG C of hydro carbons composition, heavy distillat can go expanded bed hydrogenation process to carry out lighting.

The present invention, further, (1) in air flow bed vaporescence D1, the coal gas of origin self-heating solution preocess AR10, which serves as, to be contained The material FG of gas is contacted with hydrocarbon material FS01；

In pyrolytic process AR10, vaporizes residue slag charge D1-PS or it is cooled and shaped or the conversion of its molding mass atomized particles material For the thermal decomposition product AR10P being made of coal gas, tar steam, semicoke, including air-flow is removed in the logistics of gas phase in thermal decomposition product AR10P Bed vaporescence D1 is used as the material FG containing gas.

The present invention, further, (1) in air flow bed vaporescence D1, hydrocarbon material FS01 and gassiness containing heavy hydrocarbon and/or solid The material FG of body, can carry out the air flow bed vaporescence of 2 grades or multi-stage countercurrent serial operation, and every grade of air flow bed vaporescence is equal Use air flow bed gasification burner.

The present invention, further, (1) in air flow bed vaporescence D1, hydrocarbon material FS01 and gassiness containing heavy hydrocarbon and/or solid The material FG of body, carries out the air flow bed vaporescence of 2 stage countercurrent serial operations, and every grade of air flow bed vaporescence uses air flow bed Gasification burner；

Including the hydrocarbon material FS01 of hydrocarbon and granular solids is mixed into the first gasification burner HVD-FA and the second dedirt gas D1B-PV The vaporization of first order air flow bed is completed after conjunction becomes the remaining slag charge D1A-PS of the first vaporization, and the remaining slag charge D1A-PS of the first vaporization enters Second gasification burner HVD-FB completes the vaporization of second level air flow bed after being mixed with the material FG containing gas become the remaining slag of the second vaporization Expect that D1B-PS, the remaining slag charge D1B-PS of the second vaporization are used as the remaining slag charge D1-PS of vaporization；

Material FG containing gas, which enters the second gasification burner HVD-FB, which completes the vaporization of second level air flow bed, becomes the second dust-removing gas Body D1B-PV, it is de- as first that the second dedirt gas D1B-PV enters the first gasification burner HVD-FA completion first order air flow bed vaporizations Dust and gas body D1A-PV.

The present invention, further, (1) in air flow bed vaporescence D1, hydrocarbon material FS01 and gassiness containing heavy hydrocarbon and/or solid The material FG of body, carries out the air flow bed vaporescence of 2 grades or multi-stage countercurrent serial operation, and every grade of air flow bed vaporescence uses Air flow bed gasification burner；

Light fraction oil enters in the hydrocarbon material containing heavy hydrocarbon and/or solid of air flow bed vaporescence.

4. in extraction step D1-4, vaporizing the mode of remaining slag charge D1-PS discharge air flow bed gasification burners HVD-F is：Using Mechanical pressure removal device SK will vaporize remaining slag charge D1-PS discharge air flow bed gasification burner HVD-F and expect D1- as non-stacking discharge PS-MS；

For the mechanical pressure removal device SK used for the removal device with self-sealing function, self-sealing function refers to can Prevent the gas in air flow bed gasification burner HVD-F freely with the solid mixture VS discharge air flow bed gasification burners HVD-F of oil.

The mechanical pressure removal device SK used is selected from one or more of following operating mode：

1. single-screw material discharging machine has 1 screw rod, screw rod to rotate the piston flowing to form the solid mixture VS of oil, exhaust end is matched Close arrangement material cleaner；

2. double helix material discharging machine, possesses 2 screw rods, two screw rod mutually ratcheting, mutual cleanings form the solid mixture VS of oil Piston flowing；

3. the solid mixture VS of oil is discharged the star discharge valve of star discharge valve, rotation.

The mechanical arrangement for forcing removal device SK used is selected from one or more of following operating mode：

1. being arranged in the lower part of air flow bed gasification burner HVD-F；

2. being arranged in the bottom of air flow bed gasification burner HVD-F；

3. being arranged in the bottom centre position of air flow bed gasification burner HVD-F；

4. the bottom of flash evaporation furnace HVD-F is small big under being for inverted positive cone structure, the mechanical pressure discharge of use Device SK is arranged in the bottom centre position i.e. cone tip part of flash evaporation furnace HVD-F；

5. being arranged in the bottom eccentric position of air flow bed gasification burner HVD-F；

6. the bottom of flash evaporation furnace HVD-F is small big under being for inverted eccentric pyramidal structure, the mechanical pressure row of use Glassware SK is arranged in the bottom eccentric position i.e. cone tip part of air flow bed gasification burner HVD-F.

The present invention, further, (1) in air flow bed vaporescence D1, using air flow bed gasification burner HVD-F, in air flow bed The lower part and/or bottom of gasification burner HVD-F, setting blender D1-JB is to crush oily solid material；

The power-equipment of blender D1-JB be arranged in air flow bed gasification burner HVD-F or air flow bed gasification burner HVD-F it is outer Portion, one kind or several when the power-equipment of blender D1-JB is arranged in outside air flow bed gasification burner HVD-F in following operating mode Kind：

1. air flow bed gasification burner HVD-F lower centrals position；

2. air flow bed gasification burner HVD-F lower eccentrics position；

3. the following sides air flow bed gasification burner HVD-F.

The present invention, further, (1) in air flow bed vaporescence D1, using air flow bed gasification burner HVD-F, in air flow bed Lower part in gasification burner HVD-F and/or bottom, setting scraper D1-GD are expected admittedly with removing wall oil online；

The power-equipment of scraper D1-GD be arranged in air flow bed gasification burner HVD-F or air flow bed gasification burner HVD-F it is outer Portion, one kind when power-equipment of scraper D1-GD is arranged in the outside of air flow bed gasification burner HVD-F in following operating mode or It is several：

1. air flow bed gasification burner HVD-F lower centrals position；

2. air flow bed gasification burner HVD-F lower eccentrics position；

3. the following sides air flow bed gasification burner HVD-F.

Recycling step STEP2 can be arranged in the present invention, and (1) forces discharge in air flow bed vaporescence D1, using mechanical Device SK will vaporize remaining slag charge D1-PS discharge air flow bed gasification burner HVD-F, become non-stacking discharge material D1-PS-MS；

(2) in recycling step STEP2, become using cooling and shaping device STEP2-V, non-stacking material D1-PS-MS Moulding mixture D1-PS-MS-CL；

Moulding mixture D1-PS-MS-CL discharges are cooled and shaped device STEP2-V.

Recycling step STEP2 is arranged in the present invention, and further, (2) use cooling and shaping device in recycling step STEP2 STEP2-V, cooling and shaping mode are water cooling moldings, and low-temperature cooling water, which enters, is cooled and shaped device STEP2-V, high-temperature cooling water discharge It is cooled and shaped device STEP2-V.

Recycling step STEP2 is arranged in the present invention, and further, (2) use cooling and shaping device in recycling step STEP2 STEP2-V, in the lower part and/or bottom being cooled and shaped in device STEP2-V, setting blender STEP2-JB is to crush oily solid material；

The power-equipment of blender STEP2-JB, which is arranged in, is cooled and shaped in device STEP2-V or is arranged in cooling and shaping device Outside STEP2-V, the power-equipment of blender D1-JB is arranged in when being cooled and shaped outside device STEP2-V in following operating mode It is one or more of：

1. being cooled and shaped device STEP2-V lower centrals position；

2. being cooled and shaped device STEP2-V lower eccentrics position；

3. being cooled and shaped the following sides device STEP2-V.

Recycling step STEP2 is arranged in the present invention, and further, (2) use cooling and shaping device in recycling step STEP2 STEP2-V, in the lower part and/or bottom being cooled and shaped in device STEP2-V, scraper STEP2-GD to remove wall online for setting Oily solid material；

The power-equipment of scraper STEP2-GD, which is arranged in, is cooled and shaped in device STEP2-V or is arranged in cooling and shaping device Outside STEP2-V, the power-equipment of scraper STEP2-GD is arranged in when being cooled and shaped outside device STEP2-V in following operating mode One or more：

1. being cooled and shaped device STEP2-V lower centrals position；

2. being cooled and shaped device STEP2-V lower eccentrics position；

3. being cooled and shaped the following sides device STEP2-V.

The present invention can enter hot procedure HTP based on the liquid and/or solid material of the remaining slag charge D1-PS of vaporization, Hot procedure HTP refers to vaporizing the process that remaining slag charge D1-PS carries out heat scission reaction and/or pyrogenetic reaction；

The liquid and/or solid material based on the remaining slag charge D1-PS of vaporization, are selected from the one or more of following materials：

1. the remaining slag charge D1-PS of vaporization；

2. the solid particle prepared after the remaining slag charge D1-PS cooling and solidifyings of vaporization；

3. vaporization residue slag charge D1-PS mixes the solid particle prepared after postcooling solidification with solid.

The present invention, hot procedure HTP can select one kind in following operating mode：

1. hot procedure HTP is selected from riser fluid bed heat solution preocess, gas heat carrier is used；

2. hot procedure HTP is selected from riser fluid bed heat solution preocess, solid thermal carriers are used；

3. hot procedure HTP uses fluidized wind selected from riser fluid bed heat solution preocess using solid thermal carriers.

The present invention can will be cooled and shaped device STEP2-V and force removal device SK being combined into one equipment.

The present invention can will be cooled and shaped device STEP2-V, removal device SK and air flow bed gasification burner HVD-F is forced to be combined into Integration apparatus.

The present invention can set being combined into one of condensation separator of air flow bed gasification burner HVD-F and gas D1-PV It is standby.

The present invention can set condensation separation being combined into one of tower of air flow bed gasification burner HVD-F and gas D1-PV It is standby.

The present invention, can by air flow bed gasification burner HVD-F, gas D1-PV condensation separation tower, force removal device SK, cold But being combined into one of former STEP2-V equipment.

Recycling step STEP2 is arranged in the present invention, and further, (2) use cooling and shaping device in recycling step STEP2 STEP2-V, cooling and shaping mode are water cooling moldings, and low-temperature cooling water WS, which enters, is cooled and shaped device STEP2-V, high-temperature cooling water WR Discharge is cooled and shaped device STEP2-V；

High-temperature cooling water WR is returned after cooling is cooled and shaped device STEP2-V recyclings.

It is returned as low-temperature cooling water WS after high-temperature cooling water WR filterings take off admittedly, after cooling and is cooled and shaped device STEP2- V is recycled.

Recycling step STEP2 is arranged in the present invention, and further, (2) use cooling and shaping device in recycling step STEP2 STEP2-V, cooling and shaping mode are water cooling moldings, and low-temperature cooling water, which enters, is cooled and shaped device STEP2-V, high-temperature cooling water discharge It is cooled and shaped device STEP2-V；

The discharge of the mixed material of high-temperature cooling water and moulding mixture VS-MS-CL, which is cooled and shaped device STEP2-V, becomes mixing discharge material STEP2-V-MP；

Mixing discharge material STEP2-V-MP is separated into high-temperature cooling water WR and moulding mixture VS-MS-CL；

High-temperature cooling water WR, which is returned after cooling as low-temperature cooling water WS, is cooled and shaped device STEP2-V recyclings.

Recycling step STEP2 is arranged in the present invention, and further, (2) use cooling and shaping device in recycling step STEP2 STEP2-V, cooling and shaping mode are water cooling moldings, and the operation temperature of high-temperature cooling water WR is 80~100 DEG C.

The present invention, (1) can be disposed with 1 or 2 or more in air flow bed vaporescence D1, air flow bed gasification burner HVD-F A mechanical pressure removal device SK.

The present invention, (1) can be disposed with 1 or 2 in air flow bed vaporescence D1, the bottom of air flow bed gasification burner HVD-F A or multiple vertebral bodies.

The present invention, (2) can use water-cooling type to be cooled and shaped device STEP2-V, moulding mixture VS-MS- in recycling step STEP2 The marker method of CL is intermittent.

The present invention, (2) in recycling step STEP2, the water-cooling type that uses, which is cooled and shaped device STEP2-V gas can be arranged, to be put Blank pipe STEP-P.

The present invention, (2) in recycling step STEP2, the water-cooling type used is cooled and shaped device STEP2-V setting gas blow-down pipes STEP-P；

Gas blow-down pipe STEP-P can be connected to air flow bed gasification burner HVD-F, be set on the pipeline of gas blow-down pipe STEP-P Set valve.

The present invention is cooled and shaped the spatial position of device STEP2-V, can be arranged in the lower part of air flow bed gasification burner HVD-F.

The present invention is cooled and shaped the spatial position of device STEP2-V, can be arranged under the side of air flow bed gasification burner HVD-F Portion.

The present invention, in general, (1) vaporizes the hydro carbons in remaining slag charge D1-PS mainly by routine in air flow bed vaporescence D1 The hydrocarbon component composition of the boiling point higher than 580 DEG C or higher than 530 DEG C.

The present invention, in general, (1) vaporizes the softening point of hydrocarbon in remaining slag charge D1-PS, be higher than in air flow bed vaporescence D1 120 DEG C or higher than 150 DEG C or be higher than 180 DEG C.

The present invention, as needed, (1) in air flow bed vaporescence D1, in the exhaust end for mechanically forcing removal device SK, if It is equipped with material of the material cleaner for removing exhaust end output, material cleaner is discharging version or discharging knife.

The present invention, (1) are usually in air flow bed vaporescence D1, the operating condition of air flow bed gasification burner HVD-F：Temperature is 400~550 DEG C, absolute pressure be 0.005~0.50MPa.

The present invention, (1) are generally in air flow bed vaporescence D1, the operating condition of air flow bed gasification burner HVD-F：Temperature is 450~520 DEG C, absolute pressure be 0.07~0.30MPa.

The present invention, (1) are in air flow bed vaporescence D1, the common person of operating condition of air flow bed gasification burner HVD-F：Temperature It is 0.10~0.25MPa for 470~500 DEG C, absolute pressure.

The present invention, (1) in air flow bed vaporescence D1, one or several during following of the material FG containing gas It is a：

1. the separation gas of hydrocarbon stream heating process product；

2. the pyrolysis coal gas of hydrocarbon powder, hydrocarbon powder is selected from fine coal, shale powder, oil-sand powder, other pyrolysis generation coal gas Hydrocarbon powder；

3. being pyrolyzed the gas of coal gas based on hydrocarbon powder；

4. the pyrolysis coal gas of the remaining slag charge D1-PS of vaporization；

5. the pyrolysis coal gas of the material based on the remaining slag charge D1-PS of vaporization.

Description of the drawings

Fig. 1 is the air flow bed vaporization that the heat-carrying gas air flow bed gasification method of the hydrocarbonaceous batch mixing containing solid particle of the present invention uses The 1st kind of device structure scheme of stove HVD-F is formed an airflow field, is belonged to air flow bed using a mixer, a nozzle The first basic model of gasification burner HVD-F.

As shown in Figure 1, the shell HVD-F-S of air flow bed gasification burner HVD-F is vertical gasification burner, shell HVD-F-S's Medium position, one mixer M001 of arrangement, a nozzle S001 form an airflow field obliquely, the side of nozzle S001 Border extended line is BJX01, BJX02；In general, the stream for the air flow bed that the motion process for the mixture V1P that nozzle S001 sprays is formed Field spatial dimension is more than the range that boundary line BJX01, BJX02 are included, this is the nature of the boundary flow behavior of gas jet As a result.

As shown in Figure 1, in air flow bed vaporescence D1, include the hydrocarbon material FS01 of liquid heavy hydrocarbon and granular solids, with gas Heat carrier FG completes to be mixed as mixture V1P for the first time in mixer M001, then the runner control through nozzle S001 Jetting nozzle S001 enters the inside of air flow bed gasification burner HVD-F, forms an airflow field obliquely；Why it is referred to as gas Fluidized bed is the operational volume because of the operational volume and gas heat carrier FG of the hydrocarbon material FS01 comprising liquid heavy hydrocarbon and granular solids Compared to very little, the flash process oil of hydrocarbon material FS01 or batch mixing expects to be scattered in airflow field with dispersed phase morphology admittedly.

In air flow bed vaporescence D1, includes the hydrocarbon material FS01 of liquid heavy hydrocarbon and granular solids, connect with gas heat carrier FG The evaporation for completing at least part liquid hydrocarbon SLF01-CHX is touched, the vaporization residue slag being mainly made of solid and hydrocarbon liquid is separated into Expect D1-PS and the gas D1-PV containing evaporation hydrocarbon SLF01-CHX, the evaporation of liquid hydrocarbon SLF01-CHX is by input thermal energy and/or gas Effect is proposed to be formed.

As shown in Figure 1, in air flow bed vaporescence D1, using air flow bed gasification burner HVD-F, including following work step：

1. in mixing step D1-1, hydrocarbon material FS01 and FG containing gas material is mixed into mixture V1P；Gas heat carrier FG's Operation temperature is usually above the operation temperature of hydrocarbon material FS01；

Hydrocarbon material FS01 can be pure solid-phase material, can be liquid, solid two phase materials, can be three phase materials of gas, liquid, solid；

FG containing gas material can be pure gaseous phase materials, can be two phase materials of air-liquid, can be gas, liquid, solid three-phase Material；

2. in air flow bed pervaporation step D1-2, V1P forms airflow field obliquely, solid and liquid from hydrocarbon material FS01 Fly along airflow field by injection kinetic energy and assemble after colliding gasification burner wall, is vaporized as shown in Figure 1, accumulation regions are located at air flow bed The lower part and bottom of stove HVD-F；

3. in gas solid separation step D1-3, solid settlement space is flowed upwards through after gas turns and carries out gas solid separation, Obtain dedirt gas D1-PV；Dedirt gas D1-PV is discharged by the opening K02 of the upper part of the housing air flow bed gasification burner HVD-F；

4. in extraction step D1-4, remaining slag charge D1-PS discharge air flow bed gasification burners HVD-F is vaporized；Fig. 1 show through The case where crossing opening K03 discharge air flow bed gasification burner HVD-F；Be open K03, can be the discharge of discharger such as auger stripper Mouthful.

As shown in Figure 1, there are the accumulation regions of the remaining slag charge D1-PS of vaporization in the lower part of air flow bed gasification burner HVD-F, in order to It improves the dispersion of the remaining slag charge D1-PS of vaporization, prevent the solid flitch knot of oil, in the lower space cloth of air flow bed gasification burner HVD-F Blender JB001 is set

Fig. 2 is blender JB001 detail drawings, and blender JB001 includes power end JB001-1, axis JB001-2, stirring rod JB001-3, stirring nail JB001-4.

The drive shaft JB001-2 rotations of blender JB001, power end JB001-1 as shown in Figure 1, make stirring rod JB001-3 Rotation loosens the remaining slag charge D1-PS of vaporization with stirring nail JB001-4.

Fig. 3 is the detail drawing of loading head or removal device that the present invention may use.

As shown in figure 3, arc line shaped collection flitch rotation (be shown in the figure and rotate clockwise), by the centripetal collection of bulk cargo.

As shown in figure 3, arc line shaped collection flitch rotation (rotation counterclockwise is shown in the figure), bulk cargo is pushed to outside and is received Collection.

Fig. 4 is the 2nd kind of device structure scheme for the air flow bed gasification burner HVD-F that the present invention uses, with air-flow shown in FIG. 1 Difference lies in increase the second mixer, the second nozzle being arranged symmetrically, formation 2 is cross one another to bed gasification burner HVD-F Airflow field makes the oil in air-flow expect collision to strengthen straggling effect admittedly.

As shown in figure 4,2 nozzles S001-1, S001-2 that air flow bed gasification burner HVD-F is arranged symmetrically, form 2 mutually The airflow field of intersection, the first via hydrocarbon material FS01-1 through pipeline P001-1 conveyings, the first via gas through pipeline P002-1 conveyings Heat carrier FG-1 completes to be mixed as mixture V1P-1 for the first time in mixer M001-1, then through nozzle S001-1's Runner control jetting nozzle S001-1 enters the inside of air flow bed gasification burner HVD-F, forms an airflow field obliquely；Through pipe Second road hydrocarbon material FS01-2 of road P001-2 conveyings, the first via gas heat carrier FG-2 through pipeline P002-2 conveyings are in mixer It completes to be mixed as mixture V1P-2 for the first time in M001-2, then the runner through nozzle S001-2 controls jetting nozzle S001-2 enters the inside of air flow bed gasification burner HVD-F, forms an airflow field obliquely；2 airflow fields are arranged symmetrically, phase Mutually intersect, the oil in air-flow is made to expect collision to strengthen straggling effect admittedly.

Fig. 5 is the 3rd kind of device structure scheme for the air flow bed gasification burner HVD-F that the present invention uses, air-flow as shown in fig. 4 Difference lies in increase the material scraper K005 of the vertical tube inner wall of air flow bed gasification burner HVD-F to bed gasification burner HVD-F.

Fig. 6 is scraper GD005 detail drawings, and scraper GD005 includes power end GD001-1, axis GD005-2, cross bar GD005-3, scraper GD005-4.

The drive shaft GD001-2 rotations of blender scraper GD005, power end GD001-1 as shown in Figure 5, make cross bar GD005-3 is rotated, and wipes the vaporization residue slag charge D1-PS of the vertical tube inner wall of air flow bed gasification burner HVD-F off with scraper GD005-4.

Fig. 7 is the 4th kind of device structure scheme for the air flow bed gasification burner HVD-F that the present invention uses, with air-flow shown in fig. 5 Difference lies in the middle and upper part position in air flow bed gasification burner HVD-F increases homogenizing plate K012 to bed gasification burner HVD-F； The perforated panel that flowing plate K012 is arranged horizontally can intercept the fraction solids particle in ascending air, and having to ascending air makes It is in the uniform rectified action of radial distribution.

As shown in fig. 7, the entity part of homogenizing plate K012 by K012-1, open rise hole be K012-2, the axis of scraper Set is K012-3.

The homogenizing plate of air flow bed gasification burner HVD-F settings, may be used various suitable forms, can be with vertical centre Axis is the cone plate of symmetry axis.The upper surface of homogenizing plate K012 and/or in the following, can be arranged scraper cleaning homogenizing plate K012 tables The oil of face aggregation is expected admittedly.

Fig. 8 is the 5th kind of device structure scheme for the air flow bed gasification burner HVD-F that the present invention uses, with air-flow shown in FIG. 1 Difference lies in nozzle is located at the top at the center of shell to bed gasification burner HVD-F, sprays gas downwards and is formed along under gravitational field To airflow field, airflow field is constrained by interior shell ring HVD-F-S-B；Shape between interior shell ring HVD-F-S-B and outer barrel HVD-F-S1 At the gas solid separation channel of reversing gas flow, 1 or 2 or multiple exhaust outlets are set in the upper body of outer barrel HVD-F-S1, Fig. 8 shows 2 exhaust outlets K02-1, K02-2, preferably even number exhaust outlet and Symmetric mean distribution.

As shown in figure 8, blender JB001 and scraper GD005 can share a driving equipment, driving equipment power end The bottom centre position of air flow bed gasification burner HVD-F can be located at.

Fig. 9 is the 6th kind of device structure scheme for the air flow bed gasification burner HVD-F that the present invention uses, with air-flow shown in Fig. 8 Difference lies in the absolute altitude of nozzle S001 and interior shell ring HVD-F-S-B improve bed gasification burner HVD-F, and having reduces air flow bed vaporization The effect of the vertical length of cylindrical shell sections of the outer barrel HVD-F-S1 of stove HVD-F.

Figure 10 is the 7th kind of device structure scheme for the air flow bed gasification burner HVD-F that the present invention uses, with gas shown in Fig. 9 Difference lies in the medium position of shell ring HVD-F-S-B, horizontally disposed 2 sprays of setting opposed type by fluidized bed gasification burner HVD-F Mouth S001-1, S001-2,2 airflow fields mutually impact intersection, the collision straggling effect that oil that can be in strengthening flow is expected admittedly；It is another Aspect, as shown in Figure 10, setting shell ring HVD-F-S-B inner walls deposit the Special scraper knife device GN007 that oil is expected admittedly.

Figure 11 is scraper GN007 detail drawings, and scraper GN007 includes power end GN007-1, axis GN007-2, bar GN007- 3, scraper GN007-4.

The drive shaft GN007-2 rotations of scraper GN007, power end GN007-1 as shown in Figure 10, make bar GN007-3 turn It is dynamic, the steaming residue slag charge D1-PS of shell ring HVD-F-S-B inner walls is removed with scraper GN007-4, it is made to shed into air flow bed vaporization The accumulation regions of the remaining slag charge D1-PS of steaming of the lower part of stove HVD-F.

Figure 12 is the 8th kind of device structure scheme for the air flow bed gasification burner HVD-F that the present invention uses, with gas shown in Figure 11 Difference lies in the medium position of shell ring HVD-F-S-B, 2 nozzles S001-1, S001- of setting by fluidized bed gasification burner HVD-F 2 belong to the dipping type nozzle being arranged symmetrically, and 2 airflow fields obliquely mutually impact intersection, and oil that can be in strengthening flow is expected admittedly Collision straggling effect.

Figure 13 is the 9th kind of device structure scheme for the air flow bed gasification burner HVD-F that the present invention uses, with gas shown in Figure 12 The main distinction of fluidized bed gasification burner HVD-F is, in the middle and upper part position of outer tube wall HVD-F-S1, what setting 2 was arranged symmetrically Dipping type nozzle nozzle S001-1, S001-2,2 airflow fields obliquely mutually impact intersection, and oil that can be in strengthening flow is solid The collision straggling effect of material；In the upper position of shell ring HVD-F-S-B, the floss hole of setting gas D1-PV, convenient for improving gas The height in the dedirt space of D1-PV.

Figure 14 is the inclination arrangement scheme schematic diagram for the air flow bed gasification burner HVD-F that the present invention uses, as shown in figure 14, gas Fluidized bed gasification burner HVD-F is in tilted layout, and nozzle location absolute altitude is higher than the absolute altitude of the accumulation regions of remaining slag charge D1-PS, and the program has Following advantages：

1. due to blender, scraper, auger stripper etc., slow-speed of revolution equipment, machinery and its power end such as electricity are belonged to Machine is convenient for inclination arrangement；

2. form more shell wall sides that have a down dip, can to greatest extent elimination of level face or, convenient for being arranged in apparatus casing More openings that have a down dip；

3. be easily achieved steam remaining slag charge D1-PS it is vertical under unload mode, the accumulation regions for steaming remaining slag charge D1-PS can be with shape Equipment absolute altitude is not excessively increased simultaneously at high gradient wall surface；

4. the whole absolute altitude of air flow bed gasification burner HVD-F can be reduced, it is convenient for overhaul of the equipments；

5. the absolute altitude of the condensation fractionating column of the gas D1-PV convenient for reducing downstream；

6. the absolute altitude of the cooling and shaping device of the remaining slag charge D1-PS of steaming convenient for reducing downstream；

7. the gas between condensation fractionating column convenient for shortening air flow bed gasification burner HVD-F and gas D1-PV to greatest extent Transport length and the residence time of pipeline；

8. the gas between condensation fractionating column convenient for shortening air flow bed gasification burner HVD-F and gas D1-PV to greatest extent Transport length and the residence time of pipeline；

9. convenient for air flow bed gasification burner HVD-F is set with cooling and shaping being combined into one of device for steaming remaining slag charge D1-PS It is standby；More free spaces are reserved for the top and/or top of the cooling and shaping device of the remaining slag charge D1-PS of steaming, it is remaining convenient for steaming The top of cooling and shaping device of slag charge D1-PS and/or the shell at top arrange more equipment appurtenances or opening.

Figure 15 is the 9th kind of device structure scheme for the air flow bed gasification burner HVD-F that the present invention uses, with gas shown in fig. 5 Difference lies in the medium position of shell ring HVD-F-S-B, 2 nozzles S001-1, S001- of setting by fluidized bed gasification burner HVD-F 2 belong to the updip formula nozzle being arranged symmetrically, and 2 airflow fields obliquely mutually impact intersection, and oil that can be in strengthening flow is expected admittedly Collision straggling effect.

Figure 16 is the 10th kind of device structure scheme for the air flow bed gasification burner HVD-F that the present invention uses, and can be regarded as Fig. 5 Shown in air flow bed gasification burner HVD-F shown in air flow bed gasification burner HVD-F, Figure 16 it is integrated, in shell ring HVD-F-S-B Portion position, 2 nozzles S001-1, S001-2 of setting belong to the dipping type nozzle being arranged symmetrically, 2 airflow field phases obliquely Mutually impact intersects, the collision straggling effect that oil that can be in strengthening flow is expected admittedly；In the middle and lower part position of shell ring HVD-F-S-B, if 2 nozzles S001-1, the S001-2 set belong to the updip formula nozzle being arranged symmetrically, and 2 airflow fields obliquely mutually impact friendship Fork, the collision straggling effect that oil that can be in strengthening flow is expected admittedly；The airflow field of overall 4 intersections mutually impacts intersection, can strengthen The collision straggling effect that oil in air-flow is expected admittedly.

Figure 17 is the principle schematic diagram for the three-level counter-current flow bed gasification process that the present invention uses, and uses 3 counter flow series The first gasification burner of air flow bed gasification burner HVD-FA, the second gasification burner HVD-FB, the third gasification burner HVD-FC of operation, can improve The rate of gasification of the heavy hydrocarbon of hydrocarbon material FS01, but the pressure drop of gas can be increased, therefore it is required that the pressure of heat-carrying gas air source is higher； Meanwhile vaporizing remaining slag charge and needing to enter subsequent air flow bed gasification burner, in order to increase dispersibility, the flowing of the remaining slag charge of vaporization Property, hydro carbons quantity is evaporated in hole, oily Guyuan material, intermediate raw material (i.e. intermediate vaporization residue slag charge) that can be to vaporescence step by step The hydrocarbon ils of middle addition low boiling point or moderate boiling point can effectively improve the evaporation rate of recovery of heavy hydrocarbon in liquefaction raffinate VS.

As shown in figure 17, including the hydrocarbon material FS01 of hydrocarbon and granular solids enters the first gasification burner through pipeline P001, P001A HVD-FA, which completes the vaporization of first order air flow bed, becomes the remaining slag charge D1A-PS of the first vaporization, the remaining slag charge D1A-PS warps of the first vaporization Pipeline P005A, P006B, which enter the second gasification burner HVD-FB, which completes the vaporization of second level air flow bed, becomes the remaining slag charge of the second vaporization D1B-PS, the second vaporization residue slag charge D1B-PS enter third gasification burner HVD-FC through pipeline P005B, P006C and complete the third level Air flow bed vaporization becomes third and vaporizes remaining slag charge D1C-PS.

As shown in figure 17, the material FG containing gas enters third gasification burner HVD-FC completion thirds through pipeline P002, P002C Grade air flow bed vaporization becomes third dedirt gas D1C-PV, third dedirt gas D1C-PV and enters the second vaporization through pipeline P002B Stove HVD-FB, which completes the vaporization of second level air flow bed, becomes the second dedirt gas D1B-PV, and the second dedirt gas D1B-PV is through pipeline P002A, which enters the first gasification burner HVD-FA, which completes the vaporization of first order air flow bed, becomes the first dedirt gas D1A-PV.

As shown in figure 17, light fraction oil LHCB enters the remaining slag of the vaporizations of mixing step MX9B and first through pipeline P008B Enter the second gasification burner HVD-FB after expecting D1A-PS mixing, light fraction oil LHCC enters mixing step MX9C through pipeline P008C Enter third gasification burner HVD-FC after being mixed with the second vaporization residue slag charge D1B-PS.

Figure 18 is the revolving filter schematic diagram that the discharge gas of air flow bed gasification burner HVD-F of the present invention may use, gas Body enters filter cavity by being disposed with filtering interface such as filter cloth or filter core, and solid and/or mist of oil are intercepted, and gas passes through filtering Revolving filter is flowed out behind interface；According to the gas inlet-outlet differential pressure requirements of revolving filter, the rotation update of rotating filter element wheel group Filtering interface；When old filtering interface is transferred to renewing zone, online ridding machines such as scraper, steel brush can be used to carry out interface The processing of de- deposit, wind-force purging regeneration, the deposit of collection can also be used to be discharged or draw off from renewing zone.

Figure 19 be the discharge gas of air flow bed gasification burner HVD-F of the present invention may use rotate through filter tower schematic diagram, gas Body, which enters, rotates through filter tower middle and lower part, and column plate is passed through during upper, filtering interface such as filter cloth or filter core, solid are arranged on column plate And/or mist of oil is intercepted, gas outflow after filtering interface rotates through filter tower；According to the gas inlet-outlet pressure for rotating through filter tower Difference requires, and rotating filter column plate needs to update filtering interface；When old filtering interface needs regeneration, can use online clear Except machinery such as scraper, the de- deposit processing at steel brush progress interface, wind-force purging regeneration can also be used, the deposit of collection is certainly Renewing zone is discharged or draws off.

Figure 20 is the condensing recovery process D1- of the discharge gas D1-PV for the air flow bed gasification burner HVD-F that the present invention uses The flow chart of PV-SEP.

As shown in figure 20, discharge gas D1-PV delivers into condensing recovery process D1-PV-SEP through pipeline P003, separation For mainly by normal boiling point higher than the overweight residual oil SHVD rich in solid particle that 630 DEG C of overweight the hydrocarbon component forms, mainly by Normal boiling point is less than 470 between the mink cell focus SLHD of 450~630 DEG C of heavy hydrocarbon components composition, mainly by containing normal boiling point DEG C light hydrocarbon components composition light oil SLD and primary de-oiling coal gas MQ.Condensing recovery process D1-PV-SEP, uses condensation Step, gas-liquid separation step can use the equipment such as heat exchanger, gas-liquid separator, fractionating column.

As shown in figure 20, the solid in the hydrocarbon ils material in order to reduce condensing recovery process D1-PV-SEP and/or heavy hydrocarbon contain Amount, can will be enriched in the overweight residual oil SHVD of solid particle and/or heavy hydrocarbon, and what it is as air flow bed gasification burner HVD-F " includes liquid The mixing step D1-1 and FG containing gas material of hydrocarbon material FS01 " the Returning flow bed gasification burners HVD-F of heavy hydrocarbon and/or granular solids Mixing carries out circulating vaporization separation, in this way, air flow bed gasification burner HVD-F's and condensing recovery process D1-PV-SEP constitutes group Technique is closed, integrated artistic will improve the separative efficiency of " the hydrocarbon material FS01 comprising liquid heavy hydrocarbon and/or granular solids ", can abundant profit In the air lift evaporability of gas heat carrier FG.

Flow as shown in figure 20 can use the flow of any suitable form in condensing recovery process D1-PV-SEP, can To use 1,2 high or multiple cooling steps, 1,2 high or multiple knockout drums can be used, can use 1,2 it is high or Multiple fractionating columns.

It is de- can to pass through condensation as needed by flow as shown in figure 20, the primary de-oiling coal gas MQ through pipeline P206 conveyings Water, electrically trapped tar oil, ammonia it is cold cooling de-oiling, activated carbon adsorption de-oiling, coal gas desulfurization and etc. in 1,2 or multiple steps, The different purification coal gas of property is made, the coal gas after deep purifying can be used as hydrocarbon powders flowing purification bed pyrolysis installation AR10U to make Circulating gas, for example may be used as fluidized wind, gas stripping gas etc..

Figure 21 is the fluidized bed pyrolysis device AR10U of air flow bed gasification burner HVD-F of the present invention and the remaining slag charge D1-PS of vaporization Group technology flow chart.

As shown in figure 21, the vaporization residue slag charge D1-PS of air flow bed gasification burner HVD-F discharges, enters carbon through pipeline P005 Hydrogen powders flowing purification bed pyrolysis installation AR10U.

As shown in figure 21, hydrocarbon powders flowing purification bed pyrolysis installation AR10U using fluidized bed pyrolysis reactor AR10E and usually To promote tubular type pyrolysis reactor, the fluidized bed pyrolysis reactor AR10E of hydrocarbon powders flowing purification bed pyrolysis installation AR10U is used admittedly Body heat carrier AR10KS.

As shown in figure 21, the fluid bed heat that remaining slag charge D1-PS enters hydrocarbon powders flowing purification bed pyrolysis installation AR10U is vaporized The material state for solving reactor A R10E can be that ash content containing solid, the fluid liquid containing semicoke are injected directly into solid thermal carriers The surface of AR10KS can be that the pulverized particles material of the solid being cooled into or solid is directly carried out with solid thermal carriers AR10KS Gu Gu mixing.

As shown in figure 21, the fluid bed heat that remaining slag charge D1-PS enters hydrocarbon powders flowing purification bed pyrolysis installation AR10U is vaporized The material state for solving reactor A R10E can be that the pulverized particles material of the solid being cooled into or solid is directly carried with solid thermal Body AR10KS is mixed admittedly, wherein the pulverized particles material of the solid or solid, can be mixed into solid particle such as semicoke The vaporization residue slag charge D1-PS of particle, for expanding the remaining slag charge D1-PS dispersion degrees of vaporization；At this point, it is one to be pyrolyzed hydrocarbon powder The artificial oily solid mixture of kind, may be implemented hydrocarbon and is pre-mixed admittedly, be convenient for fluidization, stream is rapidly separated conducive to pure hydrocarbon molecule is prevented It is the reaction time for controlling fluidisation pyrolysis to change pyrolysis reactor, conducive to the particle agglomeration for preventing liquid heavy hydrocarbon from causing, of course, it is possible to In the air flow bed gasification burner HVD-F for isolating the remaining slag charge D1-PS of vaporization or outside air flow bed gasification burner HVD-F, grain is set up That spends suitable semicoke particle is mixed into process, by Forced Mixing process, obtain heavy oil liquid and semicoke solid more uniformly Mixed material, then cool down the material, can be water cooling or air cooling way；The softening point of heavy resid in oily solid mixture leads to Often higher than 120 DEG C, generally greater than 150 DEG C, preferably higher than 180 DEG C；

Flow as shown in figure 21, hydrocarbon powders flowing purification bed pyrolysis installation AR10U may be used CN105602593A, CN105694933A methods and its development-oriented technique use solid thermal usually using riser fluidized bed pyrolysis reactor AR10E Carrier AR10KS (not shown in FIG.), uses fluidized wind AR10FV.

Flow as shown in figure 21, hydrocarbon powders flowing purification bed pyrolysis installation AR10U, can process simultaneously based on overweight pitch The material of SHVD.

Flow as shown in figure 21, hydrocarbon powders flowing purification bed pyrolysis installation AR10U convert vaporization residue slag charge D1-PS to Gas-solid thermal decomposition product AR10P, separation pyrolyzing product AR10P obtain pyrolysis char AR10PS and pyrolysis coal gas AR10PV；Pyrolysis half Burnt AR10PS, generally go through settler complete a degree of retardance pyrolytic reaction and deviate from the coal gas of entrainment, tar gas at For the pyrolysis char that deaerates, at least part degassing pyrolysis char, which enters to burn device and contact burn reacting with oxygenous gas, to be turned High-temperature oxydation semicoke is turned to, at least part high-temperature oxydation semicoke enters riser fluid bed heat as solid thermal carriers AR10KS The lower part for solving reactor A R10E, under fluidized wind AR10FV effects, slag charge D1-PS remaining to vaporization is carried out in the form of fluid bed Heating.

Flow as shown in figure 21, in hydrocarbon powders flowing purification bed pyrolysis installation AR10U, separation riser fluidized bed pyrolysis reaction Device AR10E thermal decomposition products AR10P obtains pyrolysis char AR10PS and pyrolysis coal gas AR10PV；Usually using can efficient removal it is small The depth gas solid separation system of particle semicoke is right as used high centrifugal force tornadotron gas-solid separator of the multitube with guide vane It is pyrolyzed coal gas AR10PV and carries out depth dedirt.

Flow as shown in figure 21, pyrolysis coal gas AR10PV is preferably pyrolysis coal gas AR10PV after depth dedirt, as coal gas 1PV enters air flow bed gasification burner HVD-F through piping 111.

Flow as shown in figure 21 can combine the other hydrocarbon powders of processing in hydrocarbon powders flowing purification bed pyrolysis installation AR10U Such as fine coal.

Figure 22 is condensing recovery process D1-PV-SEP, the vapour of air flow bed gasification burner HVD-F of the present invention, discharge gas D1-PV Change the flow chart of the group technology of the fluidized bed pyrolysis device AR10U of remaining slag charge D1-PS.

Flow as shown in figure 22, light oil distillate SLD, can deliver into hydrogenation process R20U's through pipeline P205 plus hydrogen is anti- Process R20 is answered, hydrogen supply dissolvent oil is converted into, hydrogen supply dissolvent oil can enter the hydrogenation process R30U's for using up flow type expanded bed Hydrogenation process R30 participates in Coal liquefaction.

Flow as shown in figure 22, hydrogenation process R20 can use down-type fixed-bed reactor or up flow type to fix Bed reactor or up flow type slight expanded-bed reactor or up flow type fluidized bed reactor or up flow type suspended-bed reactor or other Any appropriate form.

Flow as shown in figure 22, heavy distillate oil SLHD can be delivered into through pipeline P204 using up flow type expanded bed The hydrogenation process R30 of hydrogenation process R30U participates in Coal liquefaction, and it is molten that heavy distillate oil SLHD can be used as coal slurry to prepare Agent enters hydrogenation process R30 after being made into coal slurry pressurization with coal dust 4FM.

Flow as shown in figure 22, when R30 does not process coal dust 4FM, it is liquid catalyst that R30, which is exactly with hydrogen supply dissolvent oil DS, Heavy distillate oil SLHD's plus hydrogen lighting reaction process, a large amount of hydrogenation reaction belongs to the hydrogen migration between hydrocarbon molecule in liquid phase Reaction, overall exothermic effect is such as much smaller than the reaction heat of the aromatic hydrocarbons saturated reaction of conventional consumption molecule hydrogen and miscellaneous element The hydrogenolysis heat of sulphur, nitrogen, oxygen, therefore, overall hydrogenation reaction fuel factor is very low, is easy to use low hydrogen to oil volume ratio in this way Operating condition is to improve the liquid-phase hydrogenatin reaction efficiency of heavy distillate oil SLHD, improve reactor volume efficiency, inhibition pyrocondensation Reaction speed is closed, convenient for extending the operation cycle.

Flow as shown in figure 22 such as can routinely boil the hydrogenation process R30U of the up flow type expanded bed distillates generated O'clock between 250~450 DEG C of the hydrocarbon component, the hydrogenation process of hydrogenation process R20U is introduced as hydrogen supply hydrocarbon precursor BDS R20 is converted into the hydrogenation process R30 that hydrogen supply dissolvent oil DS returns to hydrogenation process R30U, increases hydrogen supply dissolvent oil DS total amounts.

Flow as shown in figure 22, the present invention can be using pulverized coal fluidized bed pyrolytic reaction process AR10 as the processing of starting point System, hydrogenation process R30U only process the tar that pyrolytic reaction process AR10 is generated, based on composition pyrolysis of coal " pyrolysis of coal+ The group technology of coal gas joint residue vapourizing furnace+hydrogenation of tar light hydrocarbon ", to improve the light oil of pyrolytic tar to greatest extent The cut point temperature of SLHD and SHVD can be adjusted flexibly according to R30 severe reaction conditions degree, can be reacted according to R30 for product yield The evaporation point temperature of vapourizing furnace is adjusted flexibly in condition severity.

Flow as shown in figure 22, the present invention can be using coal dust 4FM direct liquefaction hydrogenation process R30 as starting point System of processing, while the joint pyrolytic reaction for the overweight pitch SHVD of cured granulate material, pyrolytic tar for processing coal liquefaction raffinate VSP The tar that process AR10 is generated constitutes the group technology of " coal liquefaction+coal liquefaction residue pyrolysis " based on coal liquefaction, for maximum Limit improves the clean or white yield of pyrolytic tar, can be adjusted flexibly SLHD's and SHVD according to R30 severe reaction conditions degree The evaporation point temperature of vapourizing furnace can be adjusted flexibly in cut point temperature according to R30 severe reaction conditions degree.

Flow as shown in figure 22, the operating condition of each step, according to technique it needs to be determined that.

The process that coal liquefaction residue prepares cured granulate material is described below.

The present invention, the pulverized particles VSP-LS of part or all of direct hydrogenation liquefaction of coal raffinate VSP cooling obtained solid or The part or all of raffinate VSP of person mixes the powder of gained mixture VSP-ZS cooling obtained solids with solid particle ZS such as semicoke particles Broken particle VSP-ZS-LS is being converted into pyrolysis coal gas using the fluid bed riser pyrolytic reaction process AR10 of solid thermal carriers AR10PV and pyrolysis char AR10PS, recycling 1PV obtains heavy distillate oil SLHD, light oil distillate SLD, by heavy distillate oil SLHD, light oil distillate SLD or their distillate or their hydrogenated oil introduce coal dust direct liquefaction hydrogenation process R30 Processing and utilization forms group technology such as coal dust solvent naphtha with slurry, can optimize the hydrocarbon liquid feed properties of R30, extend continuous fortune The row period expands raw material coal range.

The present invention generates the vacuum distillation tower bottom of tower that the separate section of oil R30P-0 uses in direct hydrogenation liquefaction of coal, obtains To the VACUUM TOWER BOTTOM VS of material containing solid-liquid for being mainly higher than 500~540 DEG C of the hydrocarbon component by normal boiling point and solid forms, according to Soxhlet Its composition of extractive analysis is usually：

1. about 15~35% ash content [A], including inorganic matter and catalyst granules；

2. about 25~35% insoluble matter [THFI], includes the carbon skeleton tissue of non-liquefaction coal；

3. about 20~30% asphalitine, including asphaltene [HI-BS], preasphaltene [BI-THFS]；

4. about 20~30% oil [HS].

The fluidisation pyrolytic process AR10 of raffinate cured granulate material of the present invention, compared with distillation or extraction process, by routine Physical solid-liquor separation is converted into the gas solid separation of thermal decomposition product, and process goal is to recycle the pyrolysis based on oil, asphalitine Burnt oil and gas, while the high semicoke containing ash is obtained, various materials are then separately recovered, are suitable for heavy industrialization operation, it can With mating with large-scale commercial coal liquification device.

According to the present invention, the direct hydrogenation liquefaction of coal raffinate R30P-VS of liquid cool to softening point such as 100~ 150 DEG C or less can become solid, can be used similar to the molding method of coal tar pitch cooling granulation, such as direct hydrogenation liquefaction of coal Raffinate R30P-VS is after distributing device or the distribution of distributor or feed nozzle, by effective cooling procedure such as water cooling and/or wind Cold process reduces temperature and may be molded to block or pellet R30P-VS-A1S to 20~80 DEG C.

According to the present invention, it is little particulate material R30P-VS-LS that block or pellet R30P-VS-A1S, which are crushed, and grinding mode can To be that any suitable method such as rolls crushing, rolls crushing in water and then is dehydrated into dry product, dry product is by screening The particle that grain size is more than to set upper limit returns to crushing process repetition processing；The grain size of finished product little particulate material R30P-VS-LS is usual For 0~6 millimeter, generally 0~2 millimeter, preferably be 0~0.2 millimeter, in particular 0~0.02 millimeter, grain size is smaller, Time needed for pyrolytic process is shorter, but the fine particle quantity carried in coal gas can increase, this requires use that can complete The short grained depth gas solid separation system of efficient removal is as used high centrifugal force tornadotron gas-solid of the multitube with guide vane point From device.

In order to before entering fluidisation pyrolytic process, increase the dispersion of the direct hydrogenation liquefaction of coal raffinate R30P-VS of liquid Degree, increases its residence time and pyrolysis rate in pyrolysis reactor, can be by raffinate R30P-VS and solid particle ZS such as half Burnt particle is mixed to get mixture R30P-VS-ZS, the grain size of solid particle ZS is usually 0~6 millimeter, generally 0~2 millimeter, Preferably is 0~0.2 millimeter, in particular 0~0.02 millimeter；It is mixed to get the process of mixture R30P-VS-ZS, Ke Yishi Any one suitable method, for example can be the mixer mixing being arranged with pump circulation and by pipe-line system, such as can be with It is mixed with slurry kneading machine using solid.

Mixture R30P-VS-ZS cools down obtained solid R30P-VS-ZS-S, refers to mixture R30P-VS-ZS cooling drops Temperature can become solid for such as 100~150 DEG C or less to softening point, can be used similar to the molding side of coal tar pitch cooling granulation Method, for example, mixture R30P-VS-ZS by distributing device or distributor or feed nozzle distribution after, by effective cooling procedure ratio As water cooling and/or air-cooled process reduce temperature block or pellet R30P-VS-ZS-S are may be molded to 20~80 DEG C.

According to the present invention, it is little particle R30P-VS-ZS-LS that solid R30P-VS-ZS-S, which is crushed, and grinding mode can be Any suitable method such as rolls crushing, rolls crushing in water and then is dehydrated into dry product, and dry product passes through screening by grain The particle that diameter is more than set upper limit returns to crushing process repetition processing；The grain size of finished product little particle R30P-VS-ZS-LS is usually 0 ~6 millimeters, generally 0~2 millimeter, preferably be 0~0.2 millimeter, in particular 0~0.02 millimeter, grain size is smaller, pyrolysis Time needed for process is shorter, but the fine particle quantity carried in coal gas can increase, this requires use that can complete efficiently Short grained depth gas solid separation system is removed as used high centrifugal force tornadotron gas-solid separator of the multitube with guide vane.

According to the present invention, in the fluid bed riser pyrolytic reaction process AR10 using solid thermal carriers, by raffinate R30P- The cured granulate little particulate material R30P-VS-LS and/or little particle R30P-VS-ZS-LS of VS is converted into pyrolysis coal gas AR10PV and heat Solve solid AR10PS, the pyrolysis operations temperature of pyrolytic reaction process AR10 is usually 380~700 DEG C, generally 400~600 DEG C, Preferably 450~550 DEG C, the pyrolytic reaction end effector temperature of pyrolytic reaction process AR10 is usually 450~620 DEG C, is generally 510~600 DEG C, preferably 540~580 DEG C.

According to the present invention, pyrolysis coal gas is obtained in the fluid bed riser pyrolytic reaction process AR10 of solid thermal carriers AR10PV and pyrolysis solid AR10PS, recycling AR10PV can obtain tar AR10PV-DO, AR10PV-DO or its distillate or Its hydrogenated oil can introduce direct hydrogenation liquefaction of coal reaction process R30 processing and utilizations such as coal dust solvent naphtha formation group with slurry Technique is closed, the hydrocarbon liquid feed properties of R30 can be optimized, extend the continuous operation period, expand raw material coal range.

According to the present invention, pyrolysis coal gas is obtained in the fluid bed riser pyrolytic reaction process AR10 of solid thermal carriers AR10PV and pyrolysis solid AR10PS, recycling pyrolysis solid AR10PS can be used as combustion process fuel or be used as gasification Hydrocarbon material, and thermal material mode of movement may be used and realize heat integration, to improve heat utilization rate.

According to the present invention, pyrolysis coal gas is obtained in the fluid bed riser pyrolytic reaction process AR10 of solid thermal carriers AR10PV and pyrolysis solid AR10PS, recycling pyrolysis solid AR10PS, can be complete in the referred to as equipment of settler BR30E Coal gas and tar steam are pyrolyzed with abundant recycling at thorough gas solid separation, it can be in the inside of settler BR30E with suitably Tar gas, coal gas in gas stripping gas air lift pyrolysis solid AR10PS obtain degassing pyrolysis char BR30PS.

Deaerate pyrolysis char BR30PS, can be used as combustion process fuel or be used as the hydrocarbon material of gasification, and can be with Heat integration is realized using thermal material mode of movement, to improve heat utilization rate.

In system is burnt in complete pyrolysis, in general, final heat of at least part based on degassing pyrolysis char BR30PS Solution semicoke RCPS enters fluidisation and burns reaction process BR50, is contacted with oxygen-containing gas, carries out fluid bed and burns reaction BR50R, production Raw high-temperature oxydation semicoke BR50PS and flue gas YQ, flue gas YQ discharge fluidisations burn reaction process BR50；High-temperature semi-coke discharge fluidisation Burn reaction process BR50；In general, the gas solid separation process BS50 of ash-laden gas YQ, uses cyclone separator；In general, high temperature oxygen Change semicoke BR50-P1S discharge fluidisations and burns reaction process BR50；Generally, based on the BR50 high-temperature semi-coke BR50-P1S's being discharged Logistics enters pyrolytic reaction process AR10, the cured granulate little particulate material with raffinate R30P-VS as solid thermal carriers AR10KS R30P-VS-LS and/or little particle R30P-VS-ZS-LS are mixed.

The present invention can reduce or cancel VACUUM TOWER BOTTOM material containing solid-liquid VS returning to direct hydrogenation liquefaction of coal reaction process R30 As the quantity of cycle stock VS-R, thus it can significantly optimize the hydrocarbon liquid feed properties of R30, extend the continuous operation period, allow The content of ashes for adding hydrogen direct liquefaction feed coal is improved, and this point is to direct hydrogenation liquefaction of coal reaction process and its important , it is conducive to expand liquefaction coal range.

On the other hand, the utilization process of pyrolytic tar is related to condensation separation process TS, the different tar of the boiling range isolated Distillate：Overweight pitch SHVD, heavy distillate oil SLHD, light oil distillate SLD, heavy distillate oil SLHD, light oil distillate SLD Support coal liquefaction system progress hydrotreating, and the processing method of overweight pitch SHVD, it is anti-can to repeat Coal Liquefaction completely Solidification, the fluidisation method for pyrolysis of the vacuum fractionation tower bottom of tower VS of material containing solid-liquid of oil should be generated, simply method is, by overweight pitch SHVD is mixed with the vacuum fractionation tower bottom of tower VS of material containing solid-liquid and is processed.

Overweight pitch SHVD, the usually the hydrocarbon component mainly by normal boiling point higher than 580~600 DEG C are formed, and are rich in solid Grain is rich in colloid, the Gao Fang of asphalitine, low hydrogen such as containing 1~50% solid particle such as semicoke fine powder, iron rust, ash content Hydrocarbon liquid material can not use fixed bed hydrogenation technology, boiling bed hydrogenation technology, the permanently effective processing of floating bed hydrogenation technology, will surpass Heavy bitumen SHVD introduces fluid bed heat solution preocess, is a kind of Process integration technique, investment can be greatly lowered.

About hydrocarbon powders flowing purification bed pyrolysis installation AR10U, 2 kinds or a variety of hydrocarbon of the processing simultaneously in a manner of group technology When powder, processing method can select one kind of following manner, 2 kinds or a variety of：

1. 2 kinds or a variety of hydrocarbon powders, are mixed into mixture all the way, are processed together using shared pyrolysis reactor；

2. 2 kinds or a variety of hydrocarbon powders, branch enters shared pyrolysis reactor from different positions and processes together, different Feedstock hydrocarbon is not exactly the same in the path of pyrolysis reactor, but the pyrolytic reaction product of whole feedstock hydrocarbon be thoroughly mixed for 1 logistics；

3. 2 kinds or a variety of hydrocarbon powders, are processed using respective pyrolysis reactor respectively, 2 or multiple pyrolysis gas-solids production Object mixing carries out gas solid separation together；

4. 2 kinds or a variety of hydrocarbon powders, are processed using respective pyrolysis reactor respectively, 2 or multiple pyrolysis gas-solids production Object shares settler and carries out gas solid separation；

5. 2 kinds or a variety of hydrocarbon powders, are processed using respective pyrolysis reactor respectively, 2 or multiple pyrolysis gas-solids production Object shares settler and carries out gas solid separation, and the pyrolysis coal gas of 1 therein or several hydrocarbon powders enters shared settler Centre position contacts further pyrolysis with downflowing solid material；

6. 2 kinds or a variety of hydrocarbon powders are processed using respective pyrolysis reactor, settler, 2 or multiple pyrolysis respectively Semicoke, which shares, burns device；

7. 2 kinds or a variety of hydrocarbon powders, respectively using respective pyrolysis reactor, settler, burn device process, 2 or Multiple pyrolysis coal gas, which mix, carries out coal gas separation.

The present invention condensation separation process D1-PV-SEP and/or air flow bed gasification burner, can combine processing in low temperature tar or For its coal tar pitch to realize the separation of heavy distillate oil and overweight pitch, this is middle low temperature tar or the conventional distil-lation mistake of its coal tar pitch The separating effect that journey cannot achieve, the processing method of group technology can be any appropriate modes, can at least select following One kind of mode or 2 kinds：

1. middle low temperature tar or its coal tar pitch are directly mixed with coal gas 1PV or part thereof condensation de-oiling coal gas of high temperature, The part the hydrocarbon component of middle low temperature tar or its coal tar pitch is by coal gas 1PV heating and gasifyings；

2. middle low temperature tar is first separated into distillate and the lower coal tar pitch XV of initial boiling point, then coal tar pitch XV and coal gas 1PV or part thereof condenses the contact of de-oiling coal gas of high temperature.

In order to use fixed bed processing light oil distillate SLD, it may be necessary to deviate from light oil distillate using accurate filter Then de- solid rear light oil distillate SLD is introduced R20 by the entrained solid particle in SLD.

In order to use fixed bed processing light oil distillate SLD, it may be necessary to use secondary distillation process YS, lightweight is distillated Oily SLD is separated into contains solid oil SLD-MS and de- solid distilled oil SLD-L rich in solid particle, then by de- solid distilled oil SLD-L Introduce R20.

As shown in Figure 1, in order to reduce the condensation point of heavy distillate oil SLHD improve heavy distillate oil SLHD mobility or Person is in order in order to reduce the viscosity of heavy distillate oil SLHD or in order to reduce pyrocondensations of the heavy distillate oil SLHD in pyroprocess Produce rate is closed, at least part hydrogen supply dissolvent oil DS and heavy distillate oil SLHD can be conveyed and be mixed into hydrocarbon mixture SLHD-DS, mixed Close hydrocarbon SLHD-DS can go tank field store or hydrocarbon mixture SLHD-DS can after the step of being overpressurized, heating enter use The hydrogenation process R30 of up flow type expanded bed.

The discharge way of the remaining slag charge D1-PS of vaporization about gasification burner, can be any one suitable effective means, It is at least following several：

The post-production mode of the remaining slag charge D1-PS of vaporization about gasification burner, which can be any one, suitably efficacious prescriptions Formula, it is at least following several：

1. being burned in incorporation coal；

2. after being cooled and shaped, mixing and being burned in coal；Such as the lower portion of furnace body arrangement water cooling molding in gasification burner HVD-F Device or even gasification burner HVD-F can be combined into integration apparatus or system with water cooling former；

3. coking is handled；

4. pyrolysis processing, such as fluidized bed pyrolysis or the fluidized bed pyrolysis using riser；

5. with coal cocoaking processing；

6. vaporizing system coal gas uses dry powder gasification or coal-water slurry gasification；

7. being total to vaporizing system coal gas with coal, dry powder gasification or coal-water slurry gasification are used.

Specific implementation mode

The present invention described in detail below.

Pressure of the present invention, refers to absolute pressure.

Concentration of component of the present invention is weight concentration i.e. mass concentration when not specializing.

The characteristic of the present invention is described below.

3. the heavy oil discharge material of coal tar oil eliminator；

8. other solid material of oil；

9. other heavy oil material.

2. being arranged in the bottom of air flow bed gasification burner HVD-F；

1. air flow bed gasification burner HVD-F lower centrals position；

2. air flow bed gasification burner HVD-F lower eccentrics position；

3. the following sides air flow bed gasification burner HVD-F.

1. air flow bed gasification burner HVD-F lower centrals position；

2. air flow bed gasification burner HVD-F lower eccentrics position；

3. the following sides air flow bed gasification burner HVD-F.

Moulding mixture D1-PS-MS-CL discharges are cooled and shaped device STEP2-V.

1. being cooled and shaped device STEP2-V lower centrals position；

2. being cooled and shaped device STEP2-V lower eccentrics position；

3. being cooled and shaped the following sides device STEP2-V.

1. being cooled and shaped device STEP2-V lower centrals position；

2. being cooled and shaped device STEP2-V lower eccentrics position；

3. being cooled and shaped the following sides device STEP2-V.

1. the remaining slag charge D1-PS of vaporization；

1. the separation gas of hydrocarbon stream heating process product；

2. the pyrolysis coal gas of hydrocarbon powder, hydrocarbon powder is selected from fine coal, shale powder, oil-sand powder, other pyrolysis generation coal gas Hydrocarbon powder；Pyrolysis char can be used as hydrogen feedstock；

3. being pyrolyzed the gas of coal gas based on hydrocarbon powder；

4. the pyrolysis coal gas of the remaining slag charge D1-PS of vaporization；

Claims

1. the heat-carrying gas air flow bed gasification method and gasification burner of the hydrocarbon material containing heavy hydrocarbon and/or solid, it is characterised in that include following step Suddenly：

(1) in air flow bed vaporescence D1, the hydrocarbon material FS01 containing heavy hydrocarbon and/or solid is formed after being mixed with the material FG containing gas Air flow bed completes the vaporization of at least part hydrocarbon FS01-CHL, is separated into the vaporization residue slag charge being mainly made of solid and hydrocarbon liquid D1-PS and contain evaporation hydrocarbon FS01-CHL gas D1-PV；

2. spraying to form air flow bed in air flow bed pervaporation step D1-2, V1P, hydrocarbon liquid and/or solid from hydrocarbon material FS01 are by spray Kinetic energy is penetrated to fly and assemble after colliding gasification burner wall, the heavy hydrocarbon at least partially from hydrocarbon material FS01 along the flow field of air flow bed Vaporization enters in gas phase；

3. in gas solid separation step D1-3, the gas from air flow bed, which deviates from least part liquid and/or solid, becomes dust-removing gas Body D1-PV；

2. the method according to claim 11 and equipment, it is characterised in that：

(1) in air flow bed vaporescence D1, air flow bed is come from gas solid separation step D1-3 using air flow bed gasification burner HVD-F Gas turns and deviate from least part liquid and/or solid and become dedirt gas D1-PV.

3. the method according to claim 11 and equipment, it is characterised in that：

(1) it is contacted in air flow bed vaporescence D1, hydrocarbon material FS01 and the material FG containing gas and completes at least part liquid hydrocarbon The vaporization of FS01-CHL is separated into the vaporization residue slag charge D1-PS being mainly made of solid and hydrocarbon liquid and containing evaporation hydrocarbon FS01- The gas D1-PV of CHL；

1. in mixing step D1-1, the hydrocarbon material FS01 and material FG containing gas is mixed into mixture V1P, the operation temperature of material FG Higher than the operation temperature of hydrocarbon material FS01；

2. in air flow bed pervaporation step D1-2, V1P forms air flow bed, liquid from hydrocarbon material FS01 or relies on kinetic energy edge with solid It splashes and assembles in the flow field for air flow bed；

In air flow bed, the liquid hydrocarbon FS01-CHL at least part hydrocarbon material FS01 is evaporated into gas phase, may there is part High boiling hydrocarbon from the FG containing gas material enters in the remaining slag charge D1-PS of vaporization；

3. in gas turns step D1-3, gas turns carry out gas solid separation by solid settlement space, obtain dedirt gas D1- PV；

4. the method according to claim 11 and equipment, it is characterised in that：

1. in mixing step D1-1, the hydrocarbon material FS01 and material FG containing gas is mixed into mixture V1P, the material FG's containing gas Operation temperature is higher than the operation temperature of hydrocarbon material FS01；

2. in air flow bed pervaporation step D1-2, the main body initial flow direction for the air flow bed that V1P is formed is downwards or obliquely, that is, to carry out At least part is along the downward motion of gravitational field, and solid and liquid from hydrocarbon material FS01 are by kinetic energy along the flow field of air flow bed At least part is carried out along the downward motion of gravitational field and is mutually assembled；

5. method and apparatus according to claim 1 or 2 or 3 or 4, it is characterised in that：

(1) it is hot logistics in air flow bed vaporescence D1, hydrocarbon material FS01, hydrocarbon material FS01 is selected from one kind or several of following materials Kind：

3. the heavy oil discharge material of coal tar oil eliminator；

8. other solid material of oil；

9. other heavy oil material.

6. the method according to claim 11 and equipment, it is characterised in that：

(1) it is hot logistics in air flow bed vaporescence D1, hydrocarbon material FS01, temperature is 200~500 DEG C.

7. the method according to claim 11 and equipment, it is characterised in that：

(1) it is hot logistics in air flow bed vaporescence D1, hydrocarbon material FS01, temperature is 300~450 DEG C.

8. the method according to claim 11 and equipment, it is characterised in that：

(1) it is hot logistics in air flow bed vaporescence D1, hydrocarbon material FS01, temperature is 350~400 DEG C.

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

(1) contain the liquid hydrocarbon that weight concentration is 10~90% in air flow bed vaporescence D1, hydrocarbon material FS01, wherein containing weight A concentration of 3~40% normal boiling point is less than 650 DEG C of liquid hydrocarbons.

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

(1) contain the liquid hydrocarbon that weight concentration is 10~90% in air flow bed vaporescence D1, hydrocarbon material FS01, wherein containing weight A concentration of 5~30% normal boiling point is less than 650 DEG C of liquid hydrocarbons.

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

(1) contain the liquid hydrocarbon that weight concentration is 10~90% in air flow bed vaporescence D1, hydrocarbon material FS01, wherein containing weight A concentration of 8~20% normal boiling point is less than 650 DEG C of liquid hydrocarbons.

12. the method according to claim 11 and equipment, it is characterised in that：

(1) diameter of most of solid particle in air flow bed vaporescence D1, hydrocarbon material FS01 is less than 100 microns.

13. the method according to claim 11 and equipment, it is characterised in that：

(1) diameter of most of solid particle in air flow bed vaporescence D1, hydrocarbon material FS01 is less than 50 microns.

14. the method according to claim 11 and equipment, it is characterised in that：

(1) diameter of most of solid particle in air flow bed vaporescence D1, hydrocarbon material FS01 is less than 10 microns.

15. the method according to claim 11 and equipment, it is characterised in that：

(1) in air flow bed vaporescence D1, air flow bed gasification burner HVD-F is used；

1. in mixing step D1-1, hydrocarbon material FS01 and FG containing gas material is mixed into mixture V1P, and FS01 points of hydrocarbon material is 1 or 2 A or multiple branches, FG containing gas material points are 1 or 2 or multiple branches, form 1 or 2 or multiple by hydrocarbon material FS01 The mixture branch that branch is mixed into the branches of FG containing gas material.

16. the method according to claim 11 and equipment, it is characterised in that：

1. in mixing step D1-1, hydrocarbon material FS01 and FG containing gas material is mixed into mixture V1P, and FS01 points of hydrocarbon material is 1 or 2 A or multiple branches, FG containing gas material points are 1 or 2 or multiple branches, form 1 or 2 or multiple by hydrocarbon material FS01 The mixture branch that branch is mixed into the branches of FG containing gas material；

2 or multiple airflow fields intersect or liquidate and entrained oil in air-flow is made to expect to collide admittedly.

17. the method according to claim 11 and equipment, it is characterised in that：

(1) it is 400~600 DEG C in the temperature of air flow bed vaporescence D1, the FG containing gas material.

18. the method according to claim 11 and equipment, it is characterised in that：

(1) it is 450~550 DEG C in the temperature of air flow bed vaporescence D1, the FG containing gas material.

19. the method according to claim 11 and equipment, it is characterised in that：

(1) it is 480~530 DEG C in the temperature of air flow bed vaporescence D1, the FG containing gas material.

20. the method according to claim 11 and equipment, it is characterised in that：

(1) in air flow bed vaporescence D1, the hydrocarbon material FS01 containing heavy hydrocarbon and/or solid normal boiling point between 530~630 DEG C The vaporization rate of hydro carbons is more than 40%.

21. the method according to claim 11 and equipment, it is characterised in that：

(1) in air flow bed vaporescence D1, the hydrocarbon material FS01 containing heavy hydrocarbon and/or solid normal boiling point between 530~630 DEG C The vaporization rate of hydro carbons is more than 60%.

22. the method according to claim 11 and equipment, it is characterised in that：

(1) in air flow bed vaporescence D1, the hydrocarbon material FS01 containing heavy hydrocarbon and/or solid normal boiling point between 530~630 DEG C The vaporization rate of hydro carbons is more than 85%.

23. the method according to claim 11 and equipment, it is characterised in that：

(1) in air flow bed vaporescence D1, vaporize hydro carbons in remaining slag charge D1-PS mainly by normal boiling point higher than 580 DEG C or The hydrocarbon component composition higher than 530 DEG C.

24. the method according to claim 11 and equipment, it is characterised in that：

(1) in air flow bed vaporescence D1, the softening point of hydrocarbon in remaining slag charge D1-PS is vaporized, higher than 120 DEG C or higher than 150 DEG C Or it is higher than 180 DEG C.

25. the method according to claim 11 and equipment, it is characterised in that：

2. in air flow bed pervaporation step D1-2, V1P forms the air flow bed along gravitational field, solid and liquid from hydrocarbon material FS01 according to The lower part of air flow bed gasification burner HVD-F is splashed and is gathered in along the flow field of air flow bed by kinetic energy.

26. the method according to claim 11 and equipment, it is characterised in that：

In the solid settlement space, setting is disposed with the tower tray in duct, carries out rectification to upward flowing air and is uniformly distributed.

27. the method according to claim 11 and equipment, it is characterised in that：

4. in extraction step D1-4, vaporizing the mode of remaining slag charge D1-PS discharge air flow bed gasification burners HVD-F is：Using machinery Formula, which forces removal device SK that will vaporize remaining slag charge D1-PS discharge air flow bed gasification burners HVD-F, becomes non-stacking discharge material D1-PS- MS；

D1-PS-MS is expected in the non-stacking discharge, refers to that discharge material D1-PS-MS has been forced removal device SK and has carried out centainly " crushing " of degree to " the hardened property " of solid material therein so that carried out a degree of destruction.

28. the method according to claim 11 and equipment, it is characterised in that：

Dedirt gas D1-PV removes condensation fractional distillation process recycling hydrocarbon ils.

29. the method according to claim 11 and equipment, it is characterised in that：

30. the method according to claim 11 and equipment, it is characterised in that：

Dedirt gas D1-PV goes condensation fractional distillation process recycling hydrocarbon ils, recycling to obtain mainly by normal boiling point between 530~630 DEG C Hydro carbons composition the heavy distillat rich in asphaltene, preasphaltene, heavy distillat is as preparing the raw material of carbon fiber.

31. the method according to claim 11 and equipment, it is characterised in that：

Dedirt gas D1-PV goes condensation fractional distillation process recycling hydrocarbon ils, recycling to obtain mainly by normal boiling point between 530~630 DEG C Hydro carbons composition heavy distillat, heavy distillat go expanded bed hydrogenation process carry out lighting.

32. the method according to claim 11 and equipment, it is characterised in that：

(1) in air flow bed vaporescence D1, the coal gas of origin self-heating solution preocess AR10 serves as material FG and hydrocarbon material containing gas FS01 is contacted；

In pyrolytic process AR10, vaporize residue slag charge D1-PS or its cooling and shaping or its molding mass atomized particles material be converted by The thermal decomposition product AR10P of coal gas, tar steam, semicoke composition, including air flow bed vapour is removed in the logistics of gas phase in thermal decomposition product AR10P Change process D1 is used as the material FG containing gas.

33. the method according to claim 11 and equipment, it is characterised in that：

(1) in air flow bed vaporescence D1, hydrocarbon material FS01 containing the heavy hydrocarbon and/or solid and material FG containing gas, carry out 2 grades or The air flow bed vaporescence of multi-stage countercurrent serial operation, every grade of air flow bed vaporescence use air flow bed gasification burner.

34. the method according to claim 11 and equipment, it is characterised in that：

(1) in air flow bed vaporescence D1, hydrocarbon material FS01 containing the heavy hydrocarbon and/or solid and material FG containing gas, carry out 2 grades it is inverse The air flow bed vaporescence of serial operation is flowed, every grade of air flow bed vaporescence uses air flow bed gasification burner；

Including after the hydrocarbon material FS01 of hydrocarbon and granular solids is mixed into the first gasification burner HVD-FA with the second dedirt gas D1B-PV Completing the vaporization of first order air flow bed becomes the remaining slag charge D1A-PS of the first vaporization, and the remaining slag charge D1A-PS of the first vaporization enters second Gasification burner HVD-FB completes the vaporization of second level air flow bed after being mixed with the material FG containing gas become the remaining slag charge of the second vaporization D1B-PS, the remaining slag charge D1B-PS of the second vaporization are used as the remaining slag charge D1-PS of vaporization；

Material FG containing gas, which enters the second gasification burner HVD-FB, which completes the vaporization of second level air flow bed, becomes the second dedirt gas D1B-PV, the second dedirt gas D1B-PV, which enter the first gasification burner HVD-FA, which completes the vaporization of first order air flow bed, becomes the first dedirt Gas D1A-PV.

35. the method according to claim 11 and equipment, it is characterised in that：

(1) in air flow bed vaporescence D1, hydrocarbon material FS01 containing the heavy hydrocarbon and/or solid and material FG containing gas, carry out 2 grades or The air flow bed vaporescence of multi-stage countercurrent serial operation, every grade of air flow bed vaporescence use air flow bed gasification burner；

36. the method according to claim 11 and equipment, it is characterised in that：

For the removal device with self-sealing function, self-sealing function refers to prevent the mechanical pressure removal device SK used Gas in air flow bed gasification burner HVD-F is freely with the solid mixture VS discharge air flow bed gasification burners HVD-F of oil.

37. the method according to claim 11 and equipment, it is characterised in that：

1. single-screw material discharging machine has 1 screw rod, screw rod to rotate the piston flowing to form the solid mixture VS of oil, exhaust end coordinates cloth Set material cleaner；

2. double helix material discharging machine, possesses 2 screw rods, two screw rod mutually ratcheting, mutual cleanings form the work of the solid mixture VS of oil Plug flow is dynamic；

38. the method according to claim 11 and equipment, it is characterised in that：

2. being arranged in the bottom of air flow bed gasification burner HVD-F；

4. the bottom of flash evaporation furnace HVD-F is small big under being for inverted positive cone structure, the mechanical pressure removal device SK of use It is arranged in the bottom centre position i.e. cone tip part of flash evaporation furnace HVD-F；

6. the bottom of flash evaporation furnace HVD-F is small big under being for inverted eccentric pyramidal structure, the mechanical pressure removal device of use SK is arranged in the bottom eccentric position i.e. cone tip part of air flow bed gasification burner HVD-F.

39. the method according to claim 11 and equipment, it is characterised in that：

(1) in air flow bed vaporescence D1, using air flow bed gasification burner HVD-F, in the lower part of air flow bed gasification burner HVD-F and/or Bottom, setting blender D1-JB is to crush oily solid material；

The power-equipment of blender D1-JB is arranged in air flow bed gasification burner HVD-F or the outside of air flow bed gasification burner HVD-F, Selected from one or more of following operating mode when the power-equipment of blender D1-JB is arranged in outside air flow bed gasification burner HVD-F：

1. air flow bed gasification burner HVD-F lower centrals position；

2. air flow bed gasification burner HVD-F lower eccentrics position；

3. the following sides air flow bed gasification burner HVD-F.

40. the method according to claim 11 and equipment, it is characterised in that：

(1) in air flow bed vaporescence D1, using air flow bed gasification burner HVD-F, lower part in air flow bed gasification burner HVD-F and Or bottom, setting scraper D1-GD are expected admittedly with removing wall oil online；

The power-equipment of scraper D1-GD is arranged in air flow bed gasification burner HVD-F or the outside of air flow bed gasification burner HVD-F, One kind or several when the power-equipment of scraper D1-GD is arranged in the outside of air flow bed gasification burner HVD-F in following operating mode Kind：

1. air flow bed gasification burner HVD-F lower centrals position；

2. air flow bed gasification burner HVD-F lower eccentrics position；

3. the following sides air flow bed gasification burner HVD-F.

41. the method according to claim 11 and equipment, it is characterised in that：

(1) in air flow bed vaporescence D1, force removal device SK that will vaporize remaining slag charge D1-PS discharge air flow beds using mechanical Gasification burner HVD-F becomes non-stacking discharge material D1-PS-MS；

(2) in recycling step STEP2, using device STEP2-V is cooled and shaped, non-stacking material D1-PS-MS, which is cooled and shaped, becomes moulding mixture D1-PS-MS-CL；

Moulding mixture D1-PS-MS-CL discharges are cooled and shaped device STEP2-V.

42. the method according to claim 11 and equipment, it is characterised in that：

(2) in recycling step STEP2, using device STEP2-V is cooled and shaped, cooling and shaping mode is water cooling molding, sub-cooled Water, which enters, is cooled and shaped device STEP2-V, and high-temperature cooling water discharge is cooled and shaped device STEP2-V.

43. the method according to claim 11 and equipment, it is characterised in that：

(2) in recycling step STEP2, using being cooled and shaped device STEP2-V, in the lower part being cooled and shaped in device STEP2-V and/or Bottom, setting blender STEP2-JB is to crush oily solid material；

The power-equipment of blender STEP2-JB, which is arranged in be cooled and shaped in device STEP2-V or be arranged in, is cooled and shaped device STEP2- Outside V, the power-equipment of blender D1-JB be arranged in one kind when being cooled and shaped outside device STEP2-V in following operating mode or It is several：

1. being cooled and shaped device STEP2-V lower centrals position；

2. being cooled and shaped device STEP2-V lower eccentrics position；

3. being cooled and shaped the following sides device STEP2-V.

44. the method according to claim 11 and equipment, it is characterised in that：

(2) in recycling step STEP2, using being cooled and shaped device STEP2-V, in the lower part being cooled and shaped in device STEP2-V and/or Bottom, setting scraper STEP2-GD are expected admittedly with removing wall oil online；

The power-equipment of scraper STEP2-GD, which is arranged in be cooled and shaped in device STEP2-V or be arranged in, is cooled and shaped device STEP2- Outside V, the power-equipment of scraper STEP2-GD is arranged in one kind when being cooled and shaped outside device STEP2-V in following operating mode Or it is several：

1. being cooled and shaped device STEP2-V lower centrals position；

2. being cooled and shaped device STEP2-V lower eccentrics position；

3. being cooled and shaped the following sides device STEP2-V.

45. the method according to claim 11 and equipment, it is characterised in that：

Based on the liquid and/or solid material of the remaining slag charge D1-PS of vaporization, into hot procedure HTP, hot procedure HTP refers to Be process that the remaining slag charge D1-PS of vaporization carries out heat scission reaction and/or pyrogenetic reaction；

1. the remaining slag charge D1-PS of vaporization；

46. the method according to claim 11 and equipment, it is characterised in that：

Hot procedure HTP selects one kind in following operating mode：

47. the method according to claim 11 and equipment, it is characterised in that：

(1) in air flow bed vaporescence D1, the material FG containing gas is one or several during following：

1. the separation gas of hydrocarbon stream heating process product；

2. the pyrolysis coal gas of hydrocarbon powder, hydrocarbon powder is selected from fine coal, shale powder, oil-sand powder, other carbon for being pyrolyzed generation coal gas Hydrogen powder；

3. being pyrolyzed the gas of coal gas based on hydrocarbon powder；

4. the pyrolysis coal gas of the remaining slag charge D1-PS of vaporization；

48. the method according to claim 11 and equipment, it is characterised in that：

Device STEP2-V will be cooled and shaped and force removal device SK being combined into one equipment.

49. the method according to claim 11 and equipment, it is characterised in that：

Device STEP2-V will be cooled and shaped, force removal device SK and air flow bed gasification burner HVD-F being combined into one equipment.

50. the method according to claim 11 and equipment, it is characterised in that：

By condensation separator the being combined into one equipment of air flow bed gasification burner HVD-F and gas D1-PV.

51. the method according to claim 11 and equipment, it is characterised in that：

By condensation separation tower the being combined into one equipment of air flow bed gasification burner HVD-F and gas D1-PV.

52. the method according to claim 11 and equipment, it is characterised in that：

By air flow bed gasification burner HVD-F, gas D1-PV condensation separation tower, force removal device SK, be cooled and shaped device STEP2-V Being combined into one equipment.

53. the method according to claim 11 and equipment, it is characterised in that：

(2) in recycling step STEP2, using device STEP2-V is cooled and shaped, cooling and shaping mode is water cooling molding, sub-cooled Water WS, which enters, is cooled and shaped device STEP2-V, and high-temperature cooling water WR discharges are cooled and shaped device STEP2-V；

54. the method according to claim 11 and equipment, it is characterised in that：

Device STEP2-V is cooled and shaped after high-temperature cooling water WR filterings take off admittedly, after cooling as low-temperature cooling water WS returns to follow Ring uses.

55. the method according to claim 11 and equipment, it is characterised in that：

(2) in recycling step STEP2, using device STEP2-V is cooled and shaped, cooling and shaping mode is water cooling molding, sub-cooled Water, which enters, is cooled and shaped device STEP2-V, and high-temperature cooling water discharge is cooled and shaped device STEP2-V；

56. the method according to claim 11 and equipment, it is characterised in that：

(2) in recycling step STEP2, using device STEP2-V is cooled and shaped, cooling and shaping mode is water cooling molding, High-temperature cooling The operation temperature of water WR is 80~100 DEG C.

57. the method according to claim 11 and equipment, it is characterised in that：

(1) 1 or 2 or multiple mechanical pressure discharges are disposed in air flow bed vaporescence D1, air flow bed gasification burner HVD-F Device SK.

58. the method according to claim 11 and equipment, it is characterised in that：

(1) in air flow bed vaporescence D1, the bottom of air flow bed gasification burner HVD-F is disposed with 1 or 2 or multiple vertebral bodies.

59. the method according to claim 11 and equipment, it is characterised in that：

(2) in recycling step STEP2, between the marker method using water-cooling type cooling and shaping device STEP2-V, moulding mixture VS-MS-CL is It has a rest formula.

60. the method according to claim 11 and equipment, it is characterised in that：

(2) in recycling step STEP2, the water-cooling type used is cooled and shaped device STEP2-V setting gas blow-down pipes STEP-P.

61. the method according to claim 11 and equipment, it is characterised in that：

(2) in recycling step STEP2, the water-cooling type used is cooled and shaped device STEP2-V setting gas blow-down pipes STEP-P；

Gas blow-down pipe STEP-P is connected to air flow bed gasification burner HVD-F, and valve is arranged on the pipeline of gas blow-down pipe STEP-P.

62. the method according to claim 11 and equipment, it is characterised in that：

The spatial position for being cooled and shaped device STEP2-V is arranged in the lower part of air flow bed gasification burner HVD-F.

63. the method according to claim 11 and equipment, it is characterised in that：

The spatial position for being cooled and shaped device STEP2-V is arranged in the side lower part of air flow bed gasification burner HVD-F.

64. the method according to claim 11 and equipment, it is characterised in that：

(1) in air flow bed vaporescence D1, in the exhaust end for mechanically forcing removal device SK, be provided with material cleaner for remove row Expect that the material of end output, material cleaner are discharging version or discharging knife.

65. the method according to claim 11 and equipment, it is characterised in that：

(1) in air flow bed vaporescence D1, the operating condition of air flow bed gasification burner HVD-F is：Temperature is 400~550 DEG C, absolutely Pressure is 0.005~0.50MPa.

66. the method according to claim 11 and equipment, it is characterised in that：

(1) in air flow bed vaporescence D1, the operating condition of air flow bed gasification burner HVD-F is：Temperature is 450~520 DEG C, absolutely Pressure is 0.07~0.30MPa.

67. the method according to claim 11 and equipment, it is characterised in that：

(1) in air flow bed vaporescence D1, the operating condition of air flow bed gasification burner HVD-F is：Temperature is 470~500 DEG C, absolutely Pressure is 0.10~0.25MPa.