CN208964862U - A kind of adaptive three circulations pressurization carbonaceous material step conversion system - Google Patents
A kind of adaptive three circulations pressurization carbonaceous material step conversion system Download PDFInfo
- Publication number
- CN208964862U CN208964862U CN201821375259.4U CN201821375259U CN208964862U CN 208964862 U CN208964862 U CN 208964862U CN 201821375259 U CN201821375259 U CN 201821375259U CN 208964862 U CN208964862 U CN 208964862U
- Authority
- CN
- China
- Prior art keywords
- multiphase flow
- carbonaceous material
- particle
- current divider
- level
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Landscapes
- Carbon And Carbon Compounds (AREA)
- Physical Or Chemical Processes And Apparatus (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The utility model discloses a kind of adaptive three circulations pressurization carbonaceous material step conversion systems, one of adaptive three circulations pressurization carbonaceous material step reforming unit system includes carbonaceous material stock preparation system, carbonaceous material pressurization thermochemical study system, rich carbon particle chemical chain conversion system, multiphase flow separation system, apparatus system disclosed in the utility model is with petroleum coke, heavy oil sands, biomass, the carbonaceous materials such as low-rank coal resource are raw material, high-efficiency cleaning conversion and the cascade utilization of carbonaceous material can be achieved, for producing high-quality light-weight oil product and synthesis gas, New type coal can be constructed based on carbonaceous material step reforming unit system disclosed in the utility model, oil, change, electric Poly-generation mode.
Description
Technical field
The utility model belongs to derived energy chemical integrated technology and process system field, and in particular to a kind of adaptive three circulation
Pressurize carbonaceous material step conversion system.
Background technique
The clean and effective of the carbonaceous materials such as coal, biomass, petroleum coke, semicoke, oil shale, oil sands bitumen, heavy asphalt
Transformation technology be realize the diversification of industrial hydrogen production raw material, development liquid fuel synthesis, it is large can change product synthesis, fuel cell,
The polynary industries such as IGCC clean gas power generation transboundary couple the key technology, common technology, guide of the process industrials such as Industry Model
Technology.And among these, around device enlargement, adaptability to raw material is strong, technical process is intensive, efficiency of carbon con version is high, gas phase produces
Object hydrogen-carbon ratio is rationally, liquid product light component and arene content are high, device specific investment intensity is low, efficiency it is horizontal it is high, pollutant is close
Zero the targets such as puts, develop be easily industrialized popularization and application carbonaceous material it is extensive efficiently, clean the integrated dress of conversion
Set and process system by be the technical system develop important foundation stone and premise.
Patent document CN108179030A discloses a kind of biomass gasifying furnace and biomass gasification method, by being equipped with pair
Formula spout and angle formula spout are set, enables to the cross-section temperature of aditus laryngis section to be evenly distributed, and be able to maintain high temperature, so that
Tar can be aoxidized, is pyrolyzed, therefore tar removal efficiency is further enhanced in furnace.Patent document CN108003902A is public
A kind of biomass fast pyrogenation system and method for pyrolysis are opened, this method is carried using the pyrolysis gas that biomass itself generates as heat
Body and combustion gas carry out the system and method for pyrolysis of fast pyrogenation.The pyrolysis gas that biomass decomposition generates is divided into two parts, a part
It is used to heat heat carrier as the fuel of heat medium heater, after burning, another part pyrolysis gas is used directly as heat carrier,
It is passed directly into heating biological matter material in pyrolysis oven.
Patent document CN105712295A, which is disclosed, a kind of prepares porous carbon using petroleum coke and oily sludge copyrolysis
Method, the technology prepare porous carbon using petroleum coke and oily sludge copyrolysis, have played petroleum coke and oily solid sludge is assisted
Same-action to realize the recycling and innoxious use of the two, while preparing the narrow pore-size distribution with larger reference area
Porous carbon materials.Patent document CN105712295A discloses a kind of method of preparing hydrogen-rich gas by performing catalytic gasification on petroleum coke, should
After catalyst and petroleum coke are sufficiently mixed by method, gasification temperature is 700~900 DEG C, steam partial pressure is 40~70%, gas
Change the reaction time to carry out catalytic gasification reaction under the conditions of 10~120min, is removed after the coal gas export that catalytic gasification generates through condensation
Vapor is gone to finally obtain hydrogen-rich gas.
Patent document CN106010613A disclose it is a kind of by little particle oil-sand pyrolysis directly acquire light oil method and
Equipment, the utility model are crushed raw ore, are dried, and are directly cracked by high temperature, control pyrolysis time, temperature etc.
Tailings, light components to different proportion, light components are fractionated and obtain dry gas, petrol and diesel oil component, heavy oil and water.Specially
Sharp document CN106010613A discloses the method and device that a kind of oil-sand pyrolysis prepares clean fuel oil, this method by oil-sand and
Fine coal crushes, dry, mixes with high-temperature heat carrier, lime, and oil gas and semicoke are generated after pyrolytic reaction；The oil gas of generation is through cold
But, dust catching, oil gas fractionation heel row go out slurry oil, distillate and oven gas；Each distillate is clean fuel oil；Half generated
Burnt, one combust of oven gas and combustion air generates high-temperature solid particle and high-temperature flue gas；A part of conduct of high-temperature solid particle
High-temperature heat carrier, which enters, carries out pyrolytic reaction in gas retort.
As the basic energy and strategic resources in China, research is the deepest in terms of coal gasification, pyrolytic technique
Enter, traditional coal conversion is based on conversion of gasifying, and with coal gasification apparatus for " faucet ", the industrial chain in downstream has extended to coal system
Alkene, coal-ethylene glycol, is synthesized by F-T and produces fuel oil and high-end fine chemical product etc. natural gas from coal.Although coal
Gasification converts coal to CO, H of simple and stable2、CO2Equal inorganic molecules, but exist and coal molecule is excessively torn open
Point, energy consumption level is high, efficiency of energy utilization is low etc., and deficiencies, the chemical energy for failing to be contained coal resources make full use of, unreal
The now cascade utilization of the sub-prime of coal resources, classification and energy resources.And using pyrolysis of coal, dry distillation of coal technology as the modern coal of core
Charcoal resource sub-prime Efficient Conversion technology then can be achieved coal resources comprehensive utilization, it can be achieved that terminal coalification chemical product it is more
Memberization, high added value further widen the industrial chain distribution in downstream.Since Britain in 1805 passes through middle low temperature pyrogenation side first
Method using bituminous coal as raw material, start to produce semi-coke, till now, had already appeared tens of kinds of different coals heat both at home and abroad
Solution technique, external research and development are concentrated mainly on 60~seventies of last century, and representing technique mainly has the ETCH powder of the former Soviet Union
Pyrolytic process of coal, the Lurgi-Ruhrgas technique of Germany, Toscoal, COED, Garrentt technique in the U.S., Australia
The autonomous research and development of CSIR's O technique and the fast pyrolysis process of Japan etc., China's pyrolysis of coal technology starts from last century 50
Age, typical case have the DG technique of Dalian University of Technology, Anshan thermal energy institute ZNZL pyrolytic technique, the SJ pyrolytic technique in three river of Shenmu County,
The modified upgrading technology of the band oven of Beijing Collins up to company's exploitation, the GG-I moulded coal charcoal upgrading work of Beijing Guo electricity Futong exploitation
The low temperature that the heat accumulating type that skill, Beijing Shen Wu group develop is developed without heat carrier rotation bed technique, Henan Long Chengji rolling dragon at group
Retorting technique, gasification-thermal decomposition integrated technology of Shaanxi coal industry Chemical Group exploitation etc..But it is above-mentioned comprising coal, biomass,
Journey is integrated and all there is apparatus system in the transformation technology of the carbonaceous materials such as petroleum coke, semicoke, oil shale, oil sands bitumen, heavy asphalt
Spend low, efficiency it is horizontal it is low, raw material selectivity is strong, product quality is poor, it is most important that product conversion is not thorough, and is difficult carbon containing object
The terminal that material is converted into the higher high added value of yield can change product, and not realize two mistakes of carbonaceous material pyrolysis and gasification really
Journey material, energy, technical process comprehensive coupling integration, it would therefore be highly desirable to develop, a kind of adaptability to raw material is strong, product composition
Controllable, system altitude is integrated and horizontal high, the product composition of efficiency rationally, operation stability is high, system operability is strong, automatic
Change horizontal high carbonaceous material high-efficiency cleaning conversion integrated system and process.
Summary of the invention
The purpose of this utility model is to provide one kind with petroleum coke, heavy oil sands, biomass, low-rank coal resource etc.
Carbonaceous material is raw material, carries out adaptive three circulation pressurization carbonaceous material of the high-efficiency cleaning conversion with cascade utilization to carbonaceous material
Step conversion system.
In order to achieve the above objectives, the system of the utility model includes carbonaceous material stock preparation system, carbonaceous material pressurization thermalization
Learn conversion system, rich carbon particle chemical chain conversion system and multiphase flow separate system；
The carbonaceous material stock preparation system includes the carbonaceous material pretreatment sub-device being sequentially connected, carbonaceous material conveying
Device, material conveying control device and carbonaceous material stable state convey ultramagnifier；
The multiphase flow separate system includes that multiphase flow dry method dividing cell, multiphase flow quenching settler, multiphase flow are wet
Method current divider；
The multiphase flow dry method dividing cell includes that more attribute particle current dividers, level-one multiphase flow current divider, second level are more
Mutually stream current divider, three-level multiphase flow current divider；
The carbonaceous material pressurization thermochemical study system includes carbonaceous material pressurized heat chemical reaction units, carbon containing
Mixed material in the middle part of material pressurized heat chemical reaction units is strengthened to offer respectively on transmission region to be conveyed with carbonaceous material stable state
Porous active particle entrance ultramagnifier connected carbonaceous material feeding port and be connected with porous active particle returning charge unit, institute
The multiphase flow commutating zone outlet for the carbonaceous material pressurized heat chemical reaction units bottom stated is close by refractory liner and thermal capacitance/bed
Degree regulation fluidisation cycling element be connected, the top of the carbonaceous material pressurized heat chemical reaction units also with level-one multiphase flow point
Device is flowed to be connected, level-one multiphase flow current divider shunt the poor carbon particle downlink of gained successively through level-one multiphase flow current divider fluidisation dipleg,
Poor carbon particle sealing material returning device is connected with the multiphase flow temperature control region of carbonaceous material pressurized heat chemical reaction units, level-one multiphase
The high temperature gas-solid fluid-mixing of stream splitter overhead output enters second level multiphase flow current divider, second level multiphase by Lined Pipeline
Stream current divider shunts the rich carbon coarse granule downlink of gained and successively returns through second level multiphase flow current divider fluidisation dipleg, rich carbon coarse granule sealing
The circulating granular that glassware is recycled back into the rich carbon particle chemical chain reaction unit bottom of rich carbon particle chemical chain conversion system is strengthened
Transmission region, it is more that the high temperature gas-solid fluid-mixing of second level multiphase flow splitter overhead output by second level Lined Pipeline enters three-level
Mutually stream current divider, three-level multiphase flow current divider shunt the rich carbon fine grained downlink of gained and sequentially enter three-level multiphase flow current divider fluidisation
The gradation slurry preparation unit for entering after dipleg, fluidisation sinker and compound pulping agent and being connected, be made after stable suspension pump it is defeated
Into suspension slurry storage tank, suspension slurry storage tank recycles returning charge unit by the rich carbon fine grained of activity and rich carbon particle chemical chain is anti-
The chemical start of chain reaction zone of unit is answered to be connected, three-level multiphase flow current divider shunts the resulting gas-solid mixing containing ultra-fine grain
Fluid enters the multiphase flow quenching settler of multiphase flow separation system after being drawn the mixing of chilling Guan Zhongyu quenching medium；
The rich carbon particle chemical chain conversion system includes rich carbon particle chemical chain reaction unit, in rich carbon particle chemistry
The outlet of chain reaction unit lower end is provided with inert particle delivery pipe, the high temperature inert particle downlink through inert particle delivery pipe outlet
Into inert particle discharge and thermal energy recovery unit, the upper end outlet of rich carbon particle chemical chain reaction unit by Lined Pipeline with
More attribute particle current dividers are connected, and the upper end of more attribute particle current dividers is anti-by Lined Pipeline and carbonaceous material pressurization heat chemistry
The poly phase rectification area of unit lower end is answered to be connected, more attribute particle current divider lower ends are distinguished through more attribute particle current dividers fluidisation dipleg
Material returning device is sealed with porous particle and thermal capacitance/bed density regulation fluidisation cycling element is connected；
The multiphase flow quenching settler of the multiphase flow separation system, the upper end of multiphase flow quenching settler offer gas
Phase product exit, lower end are connected with the entrance of the first and second cross processing device respectively, and the outlet of the first and second cross processing device is through light
Distillate multiple-effect recovery tower is connected with multiphase flow wet process current divider, and the heavy distillate of multiphase flow wet process current divider separation is by heavy distillat
Oil export output, is advanced into colloidal solid current divider, separating obtained rich carbon colloid under obtained heavy component after shunting
Grain enters back into colloidal solid modified active tower, and the porous active particle that colloidal solid modified active tower obtains is again through porous active
Grain conveyer is recycled back into carbonaceous material pressurized heat chemical reaction units, also opens up on the side wall of colloidal solid modified active tower
There is the entrance being connected with modifying agent conveyer.
The rich carbon particle chemical chain reaction unit includes that circulating granular from bottom to top strengthens transmission region, rich carbon particle
Region of activation, chemical start of chain reaction zone, chemical chain deep reaction area and transition control region, and circulating granular strengthens transmission region side
Wall, rich carbon particle region of activation side wall, chemical start of chain reaction zone side wall offer quantity 1~10 respectively from bottom to top and pass through stream
The activator entrance that control valve is connected with activator, suspension slurry storage tank by the rich carbon fine grained of activity recycle returning charge unit with
The chemical start of chain reaction zone of rich carbon particle chemical chain reaction unit is connected.
The carbonaceous material pressurized heat chemical reaction units include multiphase flow commutating zone from bottom to top, multiphase flow temperature
Control region, mixed material strengthen transmission region and Lin Qing heat scission reaction area, and carbonaceous material entrance, porous active are granule sealed returns
Material unit strengthens transmission region with mixed material and is connected, and more attribute particle current divider fluidisation dipleg bottoms are close by thermal capacitance/bed
Degree regulation fluidisation cycling element is connected with the multiphase flow commutating zone of carbonaceous material pressurized heat chemical reaction units bottom.
Porous active particle returning charge unit include colloidal solid current divider, colloidal solid modified active tower and with colloid
Grain modified active tower connected modifying agent conveyer and porous active particle conveyer.
The rich carbon particle chemical chain reaction unit is connected with more attribute particle current dividers by Lined Pipeline, more attributes
Particle current divider fluidizes the circulation that dipleg seals material returning device and rich carbon particle chemical chain reaction unit bottom by porous particle
Grain strengthens transmission region entrance and is connected, and the axial direction of rich carbon particle chemical chain reaction unit and porous particle sealing material returning device, rich carbon
The axial angle of granule sealed material returning device is respectively 40 °~90 °.
The carbonaceous material pressurized heat chemical reaction units are connected with level-one multiphase flow current divider by Lined Pipeline, and one
Grade multiphase flow current divider fluidisation dipleg seals the more of material returning device and carbonaceous material pressurized heat chemical reaction units by poor carbon particle
Mutually stream temperature control region be connected, and the axial direction of carbonaceous material pressurized heat chemical reaction units respectively with Lined Pipeline, poor carbon particle
The axial angle for sealing material returning device is 40 °~90 °.
The three-level multiphase flow current divider middle and lower part is drawn at the top of chilling pipe outlet end and multiphase flow quenching settler
Mouthful it is connected, is drawn chilling tube inlet end the trunnion therein that is drawn is sleeved on by reducing joint and form, reducing joint and is drawn larynx
Annular chamber is formd between pipe, quenching medium is defeated through annular chamber and three-level multiphase flow current divider into chilling pipe is drawn by reducing joint
High-temperature gas-solid fluid-mixing out mixes, be drawn chilling pipe be located at three-level multiphase flow current divider tapering vertical height 1/5~
At 2/3, the angle of center line and vertical line is 30 °~65 °.
The multiphase flow quenching settler bottom is cross-like discharge port, and each discharge port passes through stop valve and the respectively
One, two cross processing devices are connected, and the outlet of the first and second cross processing device is connected after merging with light distillate multiple-effect recovery tower entrance.
The current divider Lined Pipeline is connected by thermal capacitance compensating for coupling modulator with second level Lined Pipeline.
The utility model is using the high-efficiency cleaning conversion of different carbonaceous materials and cascade utilization, the core based on the utility model
Heart integrated technique technology can be produced with high added value high-quality light-weight oil product, and construct based on light-end products deep processing and
The high-end derived energy chemical product of synthesis gas conversion synthesizes Chemical Industries chain.
Using the carbonaceous materials such as petroleum coke, heavy oil sands, biomass, low-rank coal resource as raw material, it can be achieved that carbon containing object
High-efficiency cleaning conversion and the b cascade utilization of material, for producing high-quality light-weight oil product and synthesis gas, based on the utility model, institute is public
The carbonaceous material step reforming unit system opened can construct New type coal, oil, change, electric Poly-generation mode.
Detailed description of the invention
Fig. 1 is the overall structure diagram of the utility model；
Fig. 2 is the utility model carbonaceous material pressurization thermochemical study system flow chart；
Fig. 3 is the utility model richness carbon particle chemical chain reaction cell schematics；
Fig. 4 is the utility model carbonaceous material pressurized heat chemical reaction units schematic diagram；
Fig. 5 is that the utility model is drawn chilling tube section schematic diagram.
Specific embodiment
The system and method for the utility model are described in further detail with reference to the accompanying drawing.
The system of the utility model includes carbonaceous material stock preparation system, carbonaceous material pressurization thermochemical study system, rich carbon
Particle chemical chain conversion system and multiphase flow separate system；
Referring to Fig. 1,2, carbonaceous material stock preparation system includes carbonaceous material the pretreatment sub-device 10, carbon containing object being sequentially connected
Material conveying device 11, material conveying control device 12 and carbonaceous material stable state convey ultramagnifier 13；
The multiphase flow separate system includes multiphase flow dry method dividing cell, multiphase flow quenching settler 60, multiphase flow
Wet process current divider 63；
The multiphase flow dry method dividing cell includes more attribute particle current dividers 22, level-one multiphase flow current divider 32, two
Grade multiphase flow current divider 40, three-level multiphase flow current divider 50；
The carbonaceous material pressurization thermochemical study system includes carbonaceous material pressurized heat chemical reaction units 30, is being contained
The mixed material at the middle part of carbon material pressurized heat chemical reaction units 30 is strengthened to be offered and carbonaceous material respectively on transmission region 30-3
The carbonaceous material feeding port 301 and be connected with porous active particle returning charge unit 310 more that stable state conveying ultramagnifier 13 is connected
The multiphase flow commutating zone 30-1 of hole active particle entrance 302,30 bottom of carbonaceous material pressurized heat chemical reaction units goes out
Mouth is connected by refractory liner with thermal capacitance/bed density regulation fluidisation cycling element 27, the carbonaceous material pressurization heat chemistry
The top of reaction member 30 is also connected with level-one multiphase flow current divider 32, and level-one multiphase flow current divider 32 shunts the poor carbon particle of gained
Downlink is successively through level-one multiphase flow current divider fluidisation dipleg 33, poor carbon particle sealing material returning device 34 and carbonaceous material pressurization heat chemistry
The multiphase flow temperature control region 30-2 of reaction member 30 is connected, and the high temperature gas-solid exported at the top of level-one multiphase flow current divider 32 is mixed
Collaborate body and second level multiphase flow current divider 40 is entered by Lined Pipeline 35, second level multiphase flow current divider 40 shunts rich thick of the carbon of gained
Grain downlink is successively recycled back into rich carbon particle through second level multiphase flow current divider fluidisation dipleg 41, rich carbon coarse granule sealing material returning device 42
The circulating granular of rich 20 bottom of carbon particle chemical chain reaction unit of chemical chain conversion system strengthens transmission region 20-1, second level multiphase
The high temperature gas-solid fluid-mixing exported at the top of stream current divider 40 enters three-level multiphase flow current divider by second level Lined Pipeline 43
50, three-level multiphase flow current divider 50 shunts the rich carbon fine grained downlink of gained and sequentially enters three-level multiphase flow current divider fluidisation dipleg
51, enter the gradation slurry preparation unit 53 connected with pulping agent 104 is compounded after fluidizing sinker 52, after stable suspension is made
Pump is input into suspension slurry storage tank 105, and suspension slurry storage tank 105 passes through the rich carbon fine grained of activity and recycles returning charge unit 210 and richness
The chemical start of chain reaction zone 20-3 of carbon particle chemical chain reaction unit 20 is connected, and three-level multiphase flow current divider 50 shunts resulting
Gas-solid fluid-mixing containing ultra-fine grain enters multiphase flow separation system after mixing in being drawn chilling pipe 54 with quenching medium 103
Multiphase flow quenching settler 60；
The rich carbon particle chemical chain conversion system includes rich carbon particle chemical chain reaction unit 20, in rich carbon particle
It learns the outlet of 20 lower end of chain reaction unit and is provided with inert particle delivery pipe 25, the high temperature inert through 25 outlet of inert particle delivery pipe
Inert particle discharge and thermal energy recovery unit 80 are advanced under particle, the upper end outlet of rich carbon particle chemical chain reaction unit 20 is logical
Lined Pipeline 21 is crossed to be connected with more attribute particle current dividers 22, the upper ends of more attribute particle current dividers 22 by Lined Pipeline 26 with
The poly phase rectification area of 30 lower end of carbonaceous material pressurized heat chemical reaction units is connected, and more 22 lower ends of attribute particle current divider are belonged to more
Property particle current divider fluidisation dipleg 23 to seal material returning device 24 and thermal capacitance/bed density regulation fluidisation circulation with porous particle respectively single
Member 27 is connected；
The multiphase flow quenching settler 60 of the multiphase flow separation system, the upper end of multiphase flow quenching settler 60 open up
There is gas-phase product to export 106, lower end is connected with the entrance of first and second cross processing device 61a, 61b respectively, the first and second infall
The outlet of reason device 61a, 61b are connected through light distillate multiple-effect recovery tower 62 with multiphase flow wet process current divider 63, multiphase flow wet process point
The isolated heavy distillate of device 63 is flowed by 107 output of heavy distillate outlet, is advanced into colloid under obtained heavy component after shunting
Particle current divider 64, separating obtained rich carbon colloid particle enter back into colloidal solid modified active tower 65, and colloidal solid is modified to live
Change tower 65 obtain porous active particle again through porous active particle conveyer 109, be recycled back into carbonaceous material pressurization heat chemistry
Reaction member 20 is also provided with the entrance being connected with modifying agent conveyer 108 on the side wall of colloidal solid modified active tower 65.
Referring to Fig. 3, the rich carbon particle chemical chain reaction unit 20 of the utility model is strong including circulating granular from bottom to top
Change transmission region 20-1, rich carbon particle region of activation 20-2, chemical start of chain reaction zone 20-3, chemical chain deep reaction area 20-4 and mistake
Control region 20-5 is crossed, and circulating granular reinforcing transmission region 20-1 side wall, rich carbon particle region of activation 20-2 side wall, chemical start of chain are anti-
Area's 20-3 side wall is answered to offer quantity 1~10 activation being connected by flow control valve with activator 200 respectively from bottom to top
Agent entrance, suspension slurry storage tank 105 recycle returning charge unit 210 and rich carbon particle chemical chain reaction list by the rich carbon fine grained of activity
The chemical start of chain reaction zone 20-3 of member 20 is connected.The rich carbon particle chemical chain reaction unit 20 and more attribute particles point
It flows device 22 to be connected by Lined Pipeline 21, the material leg 23 of more attribute particle current dividers 22 seals material returning device 24 by porous particle
The circulating granular of bottom of being connected with rich carbon particle chemical chain reaction unit 20 strengthens transmission region 20-1 entrance and is connected, and rich carbon particle
The center line of center line and porous particle the sealing material returning device 24 of chemical chain reaction unit 20 and rich carbon particle sealing material returning device 42
Angle is respectively 40 °~90 °.
Referring to fig. 4, the carbonaceous material pressurized heat chemical reaction units 30 of the utility model include multiphase flow from bottom to top
Commutating zone 30-1, multiphase flow temperature control region 30-2, mixed material strengthen transmission region 30-3 and Lin Qing heat scission reaction area 30-4,
And the granule sealed returning charge unit 310 of carbonaceous material entrance 301, porous active strengthens transmission region 30-3 with mixed material and is connected,
More attribute particle current divider fluidisation 23 bottoms of dipleg are added by thermal capacitance/bed density regulation fluidisation cycling element 27 with carbonaceous material
The multiphase flow commutating zone 30-1 of pressure 30 bottom of thermal chemical reaction unit is connected.The carbonaceous material pressurization thermal chemical reaction list
Member 30 is connected with before level-one multiphase flow current divider 32 by Lined Pipeline 31, and the material leg 33 of level-one multiphase flow current divider 32 is logical
Poor carbon particle sealing material returning device 34 is crossed to be connected with 30 multiphase flow temperature control region 30-2 of carbonaceous material pressurized heat chemical reaction units,
And the center line of carbonaceous material pressurized heat chemical reaction units 30 seals material returning device 34 with Lined Pipeline 31, poor carbon particle respectively
Centerlines are 40 °~90 °.
Wherein, porous active particle returning charge unit 310 includes colloidal solid current divider 64, colloidal solid modified active tower 65
And the modifying agent conveyer 108 and porous active particle conveyer 109 being connected with colloidal solid modified active tower 65.
Referring to Fig. 5,50 middle and lower part of three-level multiphase flow current divider is drawn 54 outlet end of chilling pipe and multiphase flow quenching settler
60 top entries are connected, and are drawn 54 arrival end of chilling pipe and are sleeved on by reducing joint 54-1 and therein are drawn trunnion 54-2 group
It at, reducing joint 54-1 and is drawn between trunnion 54-2 and forms annular chamber 54-3, quenching medium 103 is entered by reducing joint 54-1
It is drawn the high-temperature gas-solid fluid-mixing that chilling pipe 54 is exported through annular chamber 54-3 with three-level multiphase flow current divider 50 to mix, be drawn
Chilling pipe 54 is located at the 1/5~2/3 of 50 tapering vertical height of three-level multiphase flow current divider, and the angle of center line and vertical line is
30 °~65 °.
60 bottom of multiphase flow quenching settler of the utility model is cross-like discharge port, and each discharge port passes through respectively to be cut
Disconnected valve is connected with first and second cross processing device 61a, 61b, first and second cross processing device 61a, 61b export after merging with light fraction
Oily 62 entrance of multiple-effect recovery tower is connected.
Current divider Lined Pipeline 26 is connected by thermal capacitance compensating for coupling modulator 70 with second level Lined Pipeline 43.
Referring to Fig. 1, the course of work of the utility model includes the following steps:
A) the carbonaceous material pretreatment unit 10 that carbonaceous material 100 is introduced into carbonaceous material feed system is prepared into moisture content
After≤4.0wt%, particle size range are 100 μm~1000 μm of powder granule, then by carbonaceous material conveying device 11 and with it is defeated
Enter the mixed material of carbonaceous material pressurized heat chemical reaction units 30 after the material conveying control device 12 for sending medium 102 connected
Strengthen transmission region 30-3, high temperature gas-solid fluid-mixing generated is anti-by carbonaceous material pressurization heat chemistry after thermochemical study
It answers and is advanced into level-one multiphase flow current divider 32 on the Lin Qing heat scission reaction area 30-4 at 30 top of unit；
B) level-one multiphase flow current divider 32 shunts under the poor carbon particle that resulting carbon content is 1.00wt%~10.00wt%
It is advanced into level-one multiphase flow current divider fluidisation dipleg 33, is recycled back into carbonaceous material pressurized heat through poor carbon particle sealing material returning device 34
The multiphase flow temperature control region 30-2 of the middle and lower part of 30 bottom of chemical reaction units, the output of 32 top of level-one multiphase flow current divider
High temperature gas-solid fluid-mixing enters second level multiphase flow current divider 40 by Lined Pipeline 35；
C) second level multiphase flow current divider 40 captures particle size range >=50 μm, carbon content 50.00wt%~85.00wt%
It is advanced into second level multiphase flow current divider fluidisation dipleg 41 under rich carbon coarse granule, is recycled back into through rich carbon coarse granule sealing material returning device 42
The circulating granular of rich 20 bottom of carbon particle chemical chain reaction unit strengthens transmission region 20-1, and 40 top of second level multiphase flow current divider is defeated
High temperature gas-solid fluid-mixing out enters three-level multiphase flow current divider 50 by Lined Pipeline 43；
D) to be advanced into three-level more under 1 μm~50 μm of particle size range of the rich carbon fine grained that three-level multiphase flow current divider 50 captures
Mutually stream current divider fluidizes dipleg 51, and the rich carbon particle to flow downward in three-level multiphase flow current divider fluidisation dipleg 51 disappears by fluidisation
Stable suspension is made after entering gradating material slurry preparation unit 53 after energy device 52, retransfers into suspension slurry storage tank 105, passes through
Active richness carbon fine grained circulation returning charge unit 210 enters the chemical start of chain reaction at rich 20 middle part of carbon particle chemical chain reaction unit
Area 20-3, the gas-solid fluid-mixing exported at the top of three-level multiphase flow current divider 50 are drawn chilling pipe 54 and are mixed with quenching medium 103
Enter multiphase flow quenching settler 60 afterwards；
E) into multiphase flow quenching settler 60 gas-liquid-solid fluid-mixing carry out high efficiency shunting, gas-phase product 106 by
Output enters downstream progress depth separation at the top of multiphase flow quenching settler 60, and resulting liquid-solid multiphase product downlink is divided to two strands
Converging after into first and second cross processing device 61a, 61b into light distillate multiple-effect recovery tower 62, it is wet to finally enter multiphase flow
Multiphase flow is carried out in method current divider 63 to efficiently separate, and is advanced into colloidal solid current divider after shunting under obtained heavy component
64, separating obtained rich carbon colloid particle enters back into colloidal solid modified active tower 65 and is modified activation processing, obtained
Porous active particle passes through porous active particle conveyer 109 again and is recycled back into carbonaceous material pressurized heat chemical reaction units lower part
Mixed material strengthen transmission region 30-3；
F) circulation of rich 20 bottom of carbon particle chemical chain reaction unit is recycled back into through rich carbon coarse granule sealing material returning device 42
The rich carbon particle uplink of particle strengthening transmission region 20-1 after rich carbon particle region of activation 20-2 in step d) through active rich carbon
The stable suspension 105 that fine grained circulation returning charge unit 210 enters chemical start of chain reaction zone 20-3 merge after successively on pass through
Cross chemical chain deep reaction area 20-4 and transition control region 20-5, generated after the conversion of depth chemical chain containing more attribute particles
High temperature gas-solid fluid-mixing enters more attribute particle current dividers 22 by Lined Pipeline 21, and more attribute particle current dividers 22 shunt
More attribute particle current divider fluidisation diplegs 23 are advanced under resulting inertia coarse granule, be divided into two-way later: a-road-through is excessively porous
The circulating granular that granule sealed material returning device 24 is recycled back into rich 20 bottom of carbon particle chemical chain reaction unit strengthens transmission region 20-1,
Another way, which then passes through, is advanced into carbonaceous material pressurized heat chemical reaction units on thermal capacitance/bed density regulation fluidisation cycling element 27
30 multiphase flow commutating zone 30-1；The inertia coarse granule that rich carbon particle chemical chain reaction unit 20 generates is by outlet at bottom through discharging
Lined Pipeline 25 enters inert particle discharge and thermal energy recovery unit 80；
G) resulting high temperature gas-solid fluid-mixing is shunted through more attribute particle current dividers 22 to contain by the entrance of Lined Pipeline 26
The multiphase flow commutating zone 30-1 of 30 lowermost end of carbon material pressurized heat chemical reaction units, first and from thermal capacitance/bed density tune
It is advanced into multiphase flow temperature control region 30-2 on after more property particles rectification of flow control cycling element 27, then and from poor carbon
Mixed material is advanced on after the poor carbon particle mixing of grain sealing material returning device 34 and strengthens transmission region 30-3, finally and from carbon containing object
Enter Lin Qing heat scission reaction area 30-4 progress heat scission reaction after expecting the qualified powder granule mixing of feed system, to complete
The closed loop process of step a) to step g) recycles.
Wherein carbonaceous material 100 is the carbonaceous material of volatile matter content 20.00wt%~45.00wt%, pumped (conveying) medium 102
Using CO2、N2, one or more of oxygen content≤5.0vol% fuel combustion flue gas or circulation synthesis gas, carbonaceous material
Stable state conveys ultramagnifier 13 and is connected with the mixed material of carbonaceous material pressurized heat chemical reaction units 30 reinforcing transmission region 30-3,
It is 20~50m/s overheating protection steam that internal apparent velocity is equipped at carbonaceous material feeding port 301.
The heavy component of 63 bottom of multiphase flow wet process current divider output enters obtained solid after colloidal solid current divider 64
The colloidal solid of content 40wt%~60wt%, then can be without changing if the low aromaticity interphase of volatile content >=40wt%
Property activation and directly heat to being delivered to carbonaceous material pressurized heat chemical reaction units 30 after >=200 DEG C and carry out deep conversion.
Carbonaceous material pressurized heat chemical reaction units 30, level-one multiphase flow current divider 32, level-one multiphase flow current divider fluidisation
The poor carbon cycle revert system particle repetition factor of multichannel constructed by dipleg 23, poor carbon particle sealing material returning device 34 can 50~
Regulated and controled in the range of 300.
Activator respectively enters the rich carbon particle activation of discharge Lined Pipeline 25 and rich carbon particle chemical chain reaction unit 20
The heat chemistry chain conversion reaction of carbonaceous material is participated in after area 20-2, chemical start of chain reaction zone 20-3, wherein entering rich carbon particle
H in the activator of region of activation 20-22O (g) partial pressure and O2Intrinsic standoff ratio [(PH20)/P02] >=1.0, into chemical start of chain reaction zone
H in the activator of 20-32O (g) partial pressure and O2Intrinsic standoff ratio [(PH20)/P02]≤1.0；
The internal diameter code name of rich 20 different zones of carbon particle chemical chain reaction unit is D1, D2And D3, then circulating granular, which is strengthened, passes
It passs area 20-1 and is located at least significant end height in the range of 0.5D1~1.5D1, it is strong that rich carbon particle region of activation 20-2 is located at circulating granular
Change transmission region 20-1 upper end level as in the range of 0.5D1~1.5D1, it is living that chemical start of chain reaction zone 20-3 is located at rich carbon particle
Change area 20-2 upper end level is 0.05D2~D2In the range of, chemical chain deep reaction area 20-4 is located at chemical start of chain reaction zone
20-3 upper end level is 0.5D2~4D2In the range of, interim process control area is located at top 0.5D2~2D3In the range of.
950~1200 DEG C of operating temperature range of rich carbon particle chemical chain reaction unit (20), operating pressure be 0.5~
5MPa, internal mix fluid superficial velocity are 0.8~5.0m/s.
500~650 DEG C of operating temperature range of carbonaceous material pressurized heat chemical reaction units (30), operating pressure are
0.5~5MPa, internal mix fluid superficial velocity are 0.8~5.0m/s.
480~630 DEG C of operating temperature range of multiphase flow dry method separate system, operating pressure range is 0.5~5MPa.
280~380 DEG C of 60 operating temperature range of multiphase flow quenching settler, operating pressure are 0.5~5MPa.
80~120 DEG C of 63 operating temperature range of multiphase flow wet process current divider, operating pressure are 0.1~0.5MPa.
Low-order coal is by adaptive three circulations pressurization carbonaceous material step reforming unit system disclosed in the utility model
And after method conversion acquired middle coalite tar again successively by dedusting in subsequent coal tar pretreating process, dehydration,
Enter fractionation diced system after desalination purification and is cut into light distillate, intermediate distillates, heavy distillate for coal tar is purified；Difference evaporates
The distillate of journey enters back into subsequent distillate oil deep reforming unit system, is eventually converted into the clean fuel oil of high added value
Product, wherein light distillate is extracted for obtaining phenolic product, and dephenolize oil enters fixed bed hydrogenation unit together with intermediate distillates, weight
Distillate enters the conversion of floating bed hydrocracking unit, and the product liquid converted also enters fixed bed hydrogenation apparatus system.
Intermediate distillates, the heavy distillate produced product liquid after floating bed hydrogenation, fixed bed hydrogenation processing enter back into hydrogenation products point
From with recyclable device system, finally available LPG, hydrogen, liquid oiling product such as naphtha, diesel oil, wax oil, coal respectively
Oil, high-knock rating gasoline etc. can change product.And high hydrogen-carbon ratio synthesis gas caused by the apparatus system can not only be used for synthesizing methanol,
Ethyl alcohol, SNG, F-T synthesis can change the unstripped gas of the coals base C1 chemical industrial chain such as product, also can be used as the power generation of IGCC clean gas
Fuel gas.
Claims (9)
1. a kind of adaptive three circulations pressurization carbonaceous material step conversion system, which is characterized in that stocking up including carbonaceous material is
System, carbonaceous material pressurization thermochemical study system, rich carbon particle chemical chain conversion system and multiphase flow separate system；
The carbonaceous material stock preparation system includes carbonaceous material pretreatment sub-device (10) being sequentially connected, carbonaceous material conveying
Device (11), material conveying control device (12) and carbonaceous material stable state conveying ultramagnifier (13)；
The multiphase flow separate system includes that multiphase flow dry method dividing cell, multiphase flow quenching settler (60), multiphase flow are wet
Method current divider (63)；
The multiphase flow dry method dividing cell includes more attribute particle current dividers (22), level-one multiphase flow current divider (32), two
Grade multiphase flow current divider (40), three-level multiphase flow current divider (50)；
The carbonaceous material pressurization thermochemical study system includes carbonaceous material pressurized heat chemical reaction units (30), carbon containing
Mixed material in the middle part of material pressurized heat chemical reaction units (30) is strengthened to be offered and carbon containing object respectively on transmission region (30-3)
Expect the connected carbonaceous material feeding port (301) of stable state conveying ultramagnifier (13) and with porous active particle returning charge unit (310) phase
The porous active particle entrance (302) of connection, the multiphase flow of described carbonaceous material pressurized heat chemical reaction units (30) bottom
Commutating zone (30-1) outlet is connected by refractory liner with thermal capacitance/bed density regulation fluidisation cycling element (27), and described contains
The top of carbon material pressurized heat chemical reaction units (30) is also connected with level-one multiphase flow current divider (32), and level-one multiphase flow shunts
Device (32) shunts the poor carbon particle downlink of gained and successively seals returning charge through level-one multiphase flow current divider fluidisation dipleg (33), poor carbon particle
Device (34) is connected with the multiphase flow temperature control region (30-2) of carbonaceous material pressurized heat chemical reaction units (30), level-one multiphase flow
The high temperature gas-solid fluid-mixing exported at the top of current divider (32) enters second level multiphase flow current divider by Lined Pipeline (35)
(40), second level multiphase flow current divider (40) shunts the rich carbon coarse granule downlink of gained and successively fluidizes dipleg through second level multiphase flow current divider
(41), the rich carbon particle chemical chain that rich carbon coarse granule sealing material returning device (42) is recycled back into rich carbon particle chemical chain conversion system is anti-
The circulating granular of unit (20) bottom is answered to strengthen transmission region (20-1), the high temperature exported at the top of second level multiphase flow current divider (40)
Gas-solid fluid-mixing enters three-level multiphase flow current divider (50), three-level multiphase flow current divider by second level Lined Pipeline (43)
(50) it shunts the rich carbon fine grained downlink of gained and sequentially enters three-level multiphase flow current divider fluidisation dipleg (51), fluidisation sinker (52)
Enter the gradation slurry preparation unit (53) connected with pulping agent (104) are compounded afterwards, enters suspension material after stable suspension is made
It starches storage tank (105), suspension slurry storage tank (105) passes through rich carbon fine grained circulation returning charge unit (210) of activity and rich carbon particle
The chemical start of chain reaction zone (20-3) for learning chain reaction unit (20) is connected, and three-level multiphase flow current divider (50) shunts resulting contain
The gas-solid fluid-mixing of ultra-fine grain enters multiphase flow segregative line after mixing in being drawn chilling pipe (54) with quenching medium (103)
The multiphase flow quenching settler (60) of system；
The rich carbon particle chemical chain conversion system includes rich carbon particle chemical chain reaction unit (20), in rich carbon particle chemistry
The outlet of chain reaction unit (20) lower end is provided with inert particle delivery pipe (25), the high temperature through inert particle delivery pipe (25) outlet
Be advanced under inert particle inert particle discharge and thermal energy recovery unit (80), rich carbon particle chemical chain reaction unit (20) it is upper
It brings out mouth to be connected by Lined Pipeline (21) with more attribute particle current dividers (22), the upper end of more attribute particle current dividers (22) is logical
Current divider Lined Pipeline (26) is crossed to be connected with the poly phase rectification area of carbonaceous material pressurized heat chemical reaction units (30) lower end, it is belong to more
Property particle current divider (22) lower end through more attribute particle current dividers fluidisation dipleg (23) respectively with porous particle seal material returning device
(24) and thermal capacitance/bed density regulation fluidisation cycling element (27) is connected；
The multiphase flow quenching settler (60) of the multiphase flow separation system, the upper end of multiphase flow quenching settler (60) open up
There is gas-phase product to export (106), lower end is connected with the entrance of the first and second cross processing device (61a, 61b) respectively, and first and second hands over
The outlet of fork processor (61a, 61b) is connected through light distillate multiple-effect recovery tower (62) with multiphase flow wet process current divider (63), more
Mutually the heavy distillate of stream wet process current divider (63) separation is by heavy distillate outlet (107) output, obtained heavy group after shunting
It is advanced into colloidal solid current divider (64) under point, separating obtained rich carbon colloid particle enters back into colloidal solid modified active tower
(65), the porous active particle that colloidal solid modified active tower (65) obtains is again through porous active particle conveyer (109), circulation
It returns carbonaceous material pressurized heat chemical reaction units (30), is also provided with and changes on the side wall of colloidal solid modified active tower (65)
Property agent conveyer (108) connected entrance.
2. adaptive three circulations pressurization carbonaceous material step conversion system according to claim 1, which is characterized in that described
Rich carbon particle chemical chain reaction unit (20) include that strengthen transmission region (20-1), rich carbon particle living for circulating granular from bottom to top
Change area (20-2), chemical start of chain reaction zone (20-3), chemical chain deep reaction area (20-4) and transition control region (20-5), and
Circulating granular strengthens transmission region (20-1) side wall, rich carbon particle region of activation (20-2) side wall, chemical start of chain reaction zone (20-3)
Side wall offers quantity 1~10 activator entrance being connected by flow control valve with activator (200) respectively from bottom to top,
Suspension slurry storage tank (105) passes through rich carbon fine grained circulation returning charge unit (210) of activity and rich carbon particle chemical chain reaction unit
(20) chemical start of chain reaction zone (20-3) is connected.
3. adaptive three circulations pressurization carbonaceous material step conversion system according to claim 1, which is characterized in that described
Carbonaceous material pressurized heat chemical reaction units (30) include multiphase flow commutating zone (30-1), multiphase flow temperature tune from bottom to top
Control area (30-2), mixed material reinforcing transmission region (30-3) and Lin Qing heat scission reaction area (30-4), and carbonaceous material entrance
(301), porous active particle returning charge unit (310) strengthens transmission region (30-3) with mixed material and is connected, more attribute particles point
Stream device fluidizes dipleg (23) bottom and passes through thermal capacitance/bed density regulation fluidisation cycling element (27) and carbonaceous material pressurization heat chemistry
The multiphase flow commutating zone (30-1) of reaction member (30) bottom is connected.
4. adaptive three circulations pressurization carbonaceous material step conversion system according to claim 1, which is characterized in that porous
Active particle returning charge unit (310) includes colloidal solid current divider (64), colloidal solid modified active tower (65) and and colloid
Granule modified activation tower (65) connected modifying agent conveyer (108) and porous active particle conveyer (109).
5. adaptive three circulations pressurization carbonaceous material step conversion system according to claim 1, which is characterized in that described
Rich carbon particle chemical chain reaction unit (20) and more attribute particle current dividers (22) be connected by Lined Pipeline (21), more attributes
Particle current divider fluidizes dipleg (23) and passes through porous particle sealing material returning device (24) and rich carbon particle chemical chain reaction unit (20)
The circulating granular of bottom strengthens transmission region (20-1) entrance and is connected, and the axial direction of rich carbon particle chemical chain reaction unit (20) and more
It is respectively 40 °~90 ° that the granule sealed material returning device in hole (24), rich carbon coarse granule, which seal the axial angle of material returning device (42),.
6. adaptive three circulations pressurization carbonaceous material step conversion system according to claim 1, which is characterized in that described
Carbonaceous material pressurized heat chemical reaction units (30) and level-one multiphase flow current divider (32) be connected by Lined Pipeline (31), one
Grade multiphase flow current divider fluidisation dipleg (33) passes through poor carbon particle sealing material returning device (34) and carbonaceous material pressurization thermal chemical reaction
The multiphase flow temperature control region (30-2) of unit (30) is connected, and the axial direction of carbonaceous material pressurized heat chemical reaction units (30) point
It is not 40 °~90 ° with the axial angle of Lined Pipeline (31), poor carbon particle sealing material returning device (34).
7. adaptive three circulations pressurization carbonaceous material step conversion system according to claim 1, which is characterized in that described
Three-level multiphase flow current divider (50) middle and lower part be drawn at the top of chilling pipe (54) outlet end and multiphase flow quenching settler (60)
Mouthful it is connected, be drawn chilling pipe (54) arrival end by reducing joint (54-1) and is sleeved on and therein is drawn trunnion (54-2) group
It at, reducing joint (54-1) and is drawn between trunnion (54-2) and forms annular chamber (54-3), quenching medium (103) is by reducing joint
(54-1) is mixed into high-temperature gas-solid of the chilling pipe (54) through annular chamber (54-3) and three-level multiphase flow current divider (50) output is drawn
Interflow body mixes, and is drawn chilling pipe (54) and is located at the 1/5~2/3 of three-level multiphase flow current divider (50) tapering vertical height,
The angle of its center line and vertical line is 30 °~65 °.
8. adaptive three circulations pressurization carbonaceous material step conversion system according to claim 1, which is characterized in that described
Multiphase flow quenching settler (60) bottom be cross-like discharge port, each discharge port pass through respectively stop valve with first and second friendship
It pitches processor (61a, 61b) to be connected, the outlet of the first and second cross processing device (61a, 61b) is recycled after merging with light distillate multiple-effect
Tower (62) entrance is connected.
9. adaptive three circulations pressurization carbonaceous material step conversion system according to claim 1, it is characterised in that: described
Current divider Lined Pipeline (26) be connected with second level Lined Pipeline (43) by thermal capacitance compensating for coupling modulator (70).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201821375259.4U CN208964862U (en) | 2018-08-24 | 2018-08-24 | A kind of adaptive three circulations pressurization carbonaceous material step conversion system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201821375259.4U CN208964862U (en) | 2018-08-24 | 2018-08-24 | A kind of adaptive three circulations pressurization carbonaceous material step conversion system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN208964862U true CN208964862U (en) | 2019-06-11 |
Family
ID=66752618
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201821375259.4U Active CN208964862U (en) | 2018-08-24 | 2018-08-24 | A kind of adaptive three circulations pressurization carbonaceous material step conversion system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN208964862U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110857391A (en) * | 2018-08-24 | 2020-03-03 | 李大鹏 | Self-adaptive three-cycle pressurized carbon-containing material step conversion system and method |
-
2018
- 2018-08-24 CN CN201821375259.4U patent/CN208964862U/en active Active
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110857391A (en) * | 2018-08-24 | 2020-03-03 | 李大鹏 | Self-adaptive three-cycle pressurized carbon-containing material step conversion system and method |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102465043B (en) | Multi-section fractional pyrolysis gasification device and method for solid fuel | |
| CN101717656B (en) | Grading liquefaction method for solid fuel containing carbon and three-phase suspension bed reactor for same | |
| CN102031153B (en) | Comprehensive utilization method of oil shale | |
| CN105154121A (en) | Low-rank coal gradation usage poly-generation system and method | |
| CN103992823B (en) | Low-order coal and the method and system that biomass are Material synthesis methane and petrol and diesel oil | |
| CN103160296A (en) | Pyrolysis gasification coupling integrated poly-generation system and process for coal chemical industry | |
| US3954597A (en) | Process for the production of distillate fuels from oil shales and by-products therefrom | |
| CN101602953B (en) | Purification system of straw quick thermal cracking products | |
| CN103695057B (en) | The method of water-coal-slurry, water-coal-slurry and gasification process thereof is prepared with coal directly-liquefied residue | |
| CN102031154B (en) | Method for comprehensively utilizing lignite | |
| CN104531222B (en) | Pyrolysis of coal system and method using spouted bed reactor | |
| CN208964862U (en) | A kind of adaptive three circulations pressurization carbonaceous material step conversion system | |
| CN205133505U (en) | Low order coal grading utilizes many cogeneration system | |
| CN203159536U (en) | Coal chemical industry pyrolysis and gasification coupling integrated poly-generation system | |
| CN108251136A (en) | The classified reclaiming method of tar in a kind of hydrocarbon powders flowing purification bed pyrolysis coal gas | |
| CN103145305B (en) | Synthesis gas and synthetic natural gas or the technique and incinerator of synthetic gasoline are prepared using oily sludge | |
| CN103160305B (en) | A kind of adopt coal directly to prepare oil fuel system and technique | |
| CN209292290U (en) | A kind of oil-sand and greasy filth comprehensive utilization device | |
| CN205710607U (en) | A kind of device utilizing coke to prepare LNG unstripped gas | |
| CN105001890B (en) | A kind of coal chemical industry hydropyrolysis technique and system | |
| CN105623688A (en) | Powdered coal pyrolysis method through rapid reaction of hot carrier gas during lifting process | |
| CN209338468U (en) | A kind of comprehensive utilization device of heavy poor oil and oil shale | |
| CN204589098U (en) | Utilize the pyrolysis of coal system of spouted bed bioreactor | |
| CN108315042A (en) | A kind of coal liquefaction method preparing coal-blending coking raw material and smokeless fuel | |
| CN108148608A (en) | With the rapidly pre-warming series connection thermophilic pyrolysis hydrocarbon material method for pyrolysis of formula of Two-way Cycle powder |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |