CN110857391B

CN110857391B - Self-adaptive three-cycle pressurizing carbon-containing material cascade conversion system and method

Info

Publication number: CN110857391B
Application number: CN201810973819.4A
Authority: CN
Inventors: 李大鹏; 刘国海
Original assignee: Individual
Current assignee: Individual
Priority date: 2018-08-24
Filing date: 2018-08-24
Publication date: 2024-08-13
Anticipated expiration: 2038-08-24
Also published as: CN110857391A

Abstract

The invention discloses a self-adaptive three-cycle pressurized carbonaceous material cascade conversion device system and a method, wherein the self-adaptive three-cycle pressurized carbonaceous material cascade conversion device system comprises a carbonaceous material preparation system, a carbonaceous material pressurized thermochemical conversion system, a carbon-rich particle chemical chain conversion system and a multiphase flow separation system, and the device system and the method disclosed by the invention take carbonaceous materials such as petroleum coke, heavy oil sandstone, biomass, low-rank coal resources and the like as raw materials, can realize efficient clean conversion and cascade utilization of the carbonaceous materials, and are used for producing high-quality light oil products and synthetic gas, and the novel coal, oil, chemical and electricity multi-cogeneration modes can be constructed based on the carbonaceous material cascade conversion device system disclosed by the invention.

Description

Self-adaptive three-cycle pressurizing carbon-containing material cascade conversion system and method

Technical Field

The invention belongs to the field of energy chemical engineering integration technology and process systems, and particularly relates to a self-adaptive three-cycle pressurizing carbon-containing material step conversion system and method.

Background

The clean and efficient conversion technology of carbon-containing materials such as coal, biomass, petroleum coke, semicoke, oil shale, oil sand asphalt, heavy asphalt and the like is a key technology, a common technology and a pilot technology for realizing the diversification of industrial hydrogen production raw materials, developing multi-element industrial cross-boundary coupling industrial modes such as liquid fuel synthesis, large-scale energy product synthesis, fuel cells, IGCC clean gas power generation and the like. Wherein, the method surrounds the targets of large-scale device, strong raw material adaptability, intensive process, high carbon conversion rate, reasonable hydrogen-carbon ratio of gas phase products, high content of light components and aromatic hydrocarbons of liquid phase products, low specific investment intensity of the device, high energy efficiency level, near zero emission of pollutants and the like, the development of a large-scale efficient and clean conversion integrated device and a process system for carbon-containing materials, which are easy to realize industrialized popularization and application, is an important foundation stone and a premise for the development of the technical system.

Patent document CN108179030a discloses a biomass gasification furnace and a biomass gasification method, which can make the temperature distribution of the cross section of the throat section uniform and keep high temperature by arranging opposite nozzles and included angle nozzles, so that tar can be oxidized and pyrolyzed, and the tar removal efficiency in the furnace is further improved. Patent document CN108003902a discloses a biomass fast pyrolysis system and a pyrolysis method, and the method uses pyrolysis gas generated by biomass itself as a heat carrier and fuel gas to carry out fast pyrolysis. The pyrolysis gas generated by biomass decomposition is divided into two parts, one part is used as fuel of a heat carrier heating furnace and is used for heating the heat carrier after combustion, and the other part is directly used as the heat carrier and is directly introduced into the pyrolysis furnace for heating biomass materials.

Patent document CN105712295A discloses a method for preparing porous carbon by co-pyrolysis of petroleum coke and oil-containing sludge, which utilizes co-pyrolysis of petroleum coke and oil-containing sludge to prepare porous carbon, exerts synergistic effect of petroleum coke and oil-containing solid waste, thereby realizing recycling and harmless utilization of petroleum coke and oil-containing solid waste, and simultaneously preparing porous carbon material with narrow pore size distribution and larger comparison area. Patent document CN105712295A discloses a method for preparing hydrogen-rich gas by petroleum coke catalytic gasification, which comprises the steps of fully mixing a catalyst with petroleum coke, performing catalytic gasification reaction under the conditions of the gasification temperature of 700-900 ℃, the water vapor partial pressure of 40-70% and the gasification reaction time of 10-120 min, leading out gas generated by catalytic gasification, and removing water vapor by condensation to finally obtain the hydrogen-rich gas.

Patent document CN106010613a discloses a method and equipment for directly obtaining light oil by pyrolysis of small-particle oil sand, the invention breaks and dries raw ore, directly cracks the raw ore at high temperature, controls pyrolysis time, temperature and the like to obtain tail sand and light components with different proportions, and the light components are fractionated to obtain dry gas, gasoline and diesel components, heavy fuel oil and water. Patent document CN106010613a discloses a method and a device for preparing clean fuel oil by pyrolysis of oil sand, the method comprises the steps of crushing the oil sand and pulverized coal, drying, mixing with a high-temperature heat carrier and lime, and generating oil gas and semicoke after pyrolysis reaction; cooling the generated oil gas, trapping dust, fractionating the oil gas, and discharging slurry oil, distillate oil and coke oven gas; each distillate oil is clean fuel oil; the generated semicoke and coke oven gas are combusted together with combustion air to generate high-temperature solid particles and high-temperature flue gas; and (3) taking a part of the high-temperature solid particles as a high-temperature heat carrier to enter a carbonization furnace for pyrolysis reaction.

As basic energy and strategic resources in China, the gasification and pyrolysis technologies of coal are most widely and deeply studied, the traditional coal conversion is mainly carried out by gasification, a coal gasification device is used as a tap, and the downstream industrial chain is expanded to coal-to-olefin, coal-to-natural gas, coal-to-glycol, and fuel oil products and high-end fine chemical products prepared by F-T synthesis. Although coal gasification converts coal into simple and stable inorganic micromolecules such as CO, H ₂、CO₂ and the like, the defects of excessive splitting of coal molecules, high energy consumption level, low energy utilization efficiency and the like exist, chemical energy contained in coal resources cannot be fully utilized, and quality and classification of the coal resources and cascade utilization of the energy resources are not realized. The modern coal resource quality-dividing and high-efficiency conversion process technology taking the coal pyrolysis and coal carbonization technology as the core can realize the comprehensive utilization of coal resources, can realize the diversification and high added value of terminal coal chemical products, and further widens the downstream industrial chain distribution. Since 1805 uk starts by using bituminous coal as raw material through middle-low temperature pyrolysis method, so far, tens of different coal pyrolysis processes have appeared at home and abroad, research and development mainly concentrate on the last 60-70 years, representing processes mainly including the process of the three-in-one ETCH pulverized coal pyrolysis, the Lurgi-Ruhrgas process in germany, the Toscoal, COED, garrentt process in the united states, the CSIRO process in australia, the fast pyrolysis process in japan, etc., autonomous research and development of the coal pyrolysis technology starts in the last 50 years, typically the DG process in the university of the major connecting industry, the ZNZL pyrolysis technology in the heat energy institute of the saddle mountain, the SJ pyrolysis technology in the three rivers of the god, the modified upgrading technology of the belt furnace developed by the company of the hollye, the GG-I type coal upgrading technology developed by the electric rich communication of the beijing country, the heat accumulating type athermal carrier rotating bed technology developed by the group of the Beijing god fog group, the low temperature technology developed by the group of the dragon in south, the gasification integrated pyrolysis technology developed by the group of the chemical industry in the gasification of the western industry, etc. However, the above-mentioned conversion technologies for carbonaceous materials including coal, biomass, petroleum coke, semicoke, oil shale, oil sand asphalt, heavy asphalt and the like all have the advantages of low system integration degree, low energy efficiency level, strong raw material selectivity, poor product quality, and most importantly, the product conversion is incomplete, the carbonaceous materials are difficult to be converted into high-value-added terminal energy products with higher yield, and comprehensive coupling integration of two processes of pyrolysis and gasification of the carbonaceous materials in the material, energy and technological process is not really realized, so the development of an efficient clean conversion integrated system and technological method for the carbonaceous materials, which have the advantages of strong raw material adaptability, adjustable product composition, high system integration, reasonable product composition, high operation stability, strong system operability and high automation level, are needed to be developed.

Disclosure of Invention

The invention aims to provide a self-adaptive three-cycle pressurizing carbon-containing material cascade conversion system and method for efficiently and cleanly converting and cascade utilizing carbon-containing materials by taking petroleum coke, heavy oil sandstone, biomass, low-rank coal resources and the like as raw materials.

In order to achieve the above purpose, the system of the invention comprises a carbonaceous material preparation system, a carbonaceous material pressurized thermochemical conversion system, a carbon-rich particle chemical chain conversion system and a multiphase flow diversion system;

The carbonaceous material preparation system comprises a carbonaceous material pretreatment sub-device, a carbonaceous material conveying device, a material conveying control device and a carbonaceous material steady-state conveying feedback device which are sequentially connected;

The multiphase flow diversion system comprises a multiphase flow dry diversion unit, a multiphase flow quenching settler and a multiphase flow wet diversion device;

The multiphase flow dry diversion unit comprises a multi-attribute particle diverter, a first-stage multiphase flow diverter, a second-stage multiphase flow diverter and a third-stage multiphase flow diverter;

The carbonaceous material pressurized thermochemical conversion system comprises a carbonaceous material pressurized thermochemical reaction unit, a carbonaceous material feeding port connected with a carbonaceous material steady-state conveying feedback device and a porous active particle inlet connected with a porous active particle returning unit are respectively arranged on a mixed material enhanced transfer area in the middle part of the carbonaceous material pressurized thermochemical reaction unit, a multiphase flow rectifying area outlet at the bottom of the carbonaceous material pressurized thermochemical reaction unit is connected with a heat capacity/bed density regulation fluidization circulating unit through a refractory lining, the top of the carbonaceous material pressurized thermochemical reaction unit is also connected with a first-stage multiphase flow splitter, lean carbon particles obtained by the split flow of the first-stage multiphase flow splitter are sequentially connected with a multiphase flow temperature regulation area of the carbonaceous material pressurized thermochemical reaction unit through a first-stage multiphase flow splitter fluidization material leg and a lean carbon particle sealing return device, high-temperature gas-solid mixed fluid output from the top of the first-stage multiphase flow splitter enters a second-stage multiphase flow splitter through a lining pipeline, the rich carbon coarse particles obtained by the split flow of the second-stage multiphase flow splitter enter a second-stage multi-phase flow splitter sealing fluid return device to be sequentially connected with a slurry preparation pump, and the slurry is sequentially prepared into a third-stage slurry storage tank after entering the high-stage fluid slurry, and the slurry is sequentially connected with the third-stage slurry high-stage slurry phase flow splitter, the suspension slurry storage tank is connected with a chemical chain initial reaction zone of the carbon-rich particle chemical chain reaction unit through an active carbon-rich fine particle circulating and returning unit, and gas-solid mixed fluid containing ultrafine particles, which is obtained by shunting by a three-stage multiphase flow diverter, enters a multiphase flow quenching settler of a multiphase flow separation system after being mixed with a quenching agent in a pumping quenching pipe;

the carbon-rich particle chemical chain conversion system comprises a carbon-rich particle chemical chain reaction unit, an inert particle discharge pipe is arranged at an outlet at the lower end of the carbon-rich particle chemical chain reaction unit, high-temperature inert particles discharged from the inert particle discharge pipe travel into an inert particle discharge and heat energy recovery unit, an outlet at the upper end of the carbon-rich particle chemical chain reaction unit is connected with a multi-attribute particle diverter through a lining pipeline, the upper end of the multi-attribute particle diverter is connected with a multiphase rectification zone at the lower end of a carbonaceous material pressurizing thermochemical reaction unit through the lining pipeline, and the lower end of the multi-attribute particle diverter is connected with a porous particle sealing material returning device and a heat capacity/bed density regulating fluidization circulation unit through fluidization material legs of the multi-attribute particle diverter;

The multiphase flow quenching settler of the multiphase flow separation system is characterized in that the upper end of the multiphase flow quenching settler is provided with a gas-phase product outlet, the lower end of the multiphase flow quenching settler is respectively connected with inlets of a first cross processor and a second cross processor, the outlets of the first cross processor and the second cross processor are connected with a multiphase flow wet splitter through a light distillate oil multi-effect recovery tower, heavy distillate oil separated by the multiphase flow wet splitter is output through a heavy distillate oil outlet, heavy components obtained after splitting flow down enter a colloid particle splitter, carbon-rich colloid particles obtained after splitting enter a colloid particle modification activation tower again, porous active particles obtained by the colloid particle modification activation tower are circularly returned to a carbonaceous material pressurizing thermochemical reaction unit through a porous active particle conveyor, and an inlet connected with a modifier conveyor is further formed in the side wall of the colloid particle modification activation tower.

The carbon-rich particle chemical chain reaction unit comprises a circulating particle reinforced transfer area, a carbon-rich particle activation area, a chemical chain initial reaction area, a chemical chain deep reaction area and a transition regulation area from bottom to top, wherein 1-10 activator inlets connected with an activator through a flow control valve are respectively formed in the side wall of the circulating particle reinforced transfer area, the side wall of the carbon-rich particle activation area and the side wall of the chemical chain initial reaction area from bottom to top, and a suspension slurry storage tank is connected with the chemical chain initial reaction area of the carbon-rich particle chemical chain reaction unit through an active carbon-rich fine particle circulating returning unit.

The carbonaceous material pressurizing thermochemical reaction unit comprises a multiphase flow rectifying area, a multiphase flow temperature regulating area, a mixed material strengthening transfer area and a hydro-thermal cracking reaction area from bottom to top, a carbonaceous material inlet and a porous active particle sealing returning unit are communicated with the mixed material strengthening transfer area, and the bottom of a fluidization dipleg of the multi-attribute particle diverter is connected with the multiphase flow rectifying area at the bottom of the carbonaceous material pressurizing thermochemical reaction unit through a heat capacity/bed density regulating and fluidization circulating unit.

The porous active particle returning unit comprises a colloid particle diverter, a colloid particle modifying and activating tower, and a modifier conveyor and a porous active particle conveyor which are connected with the colloid particle modifying and activating tower.

The carbon-rich particle chemical chain reaction unit is connected with the multi-attribute particle diverter through a lining pipeline, the fluidization dipleg of the multi-attribute particle diverter is connected with the inlet of the circulating particle reinforced transmission area at the bottom of the carbon-rich particle chemical chain reaction unit through the porous particle sealing return device, and the axial included angles between the axial direction of the carbon-rich particle chemical chain reaction unit and the porous particle sealing return device and between the axial direction of the carbon-rich particle chemical chain reaction unit and the axial direction of the porous particle sealing return device are respectively 40-90 degrees.

The carbon-containing material pressurized thermochemical reaction unit is connected with the primary multiphase flow diverter through a lining pipeline, the fluidization dipleg of the primary multiphase flow diverter is connected with the multiphase flow temperature regulation area of the carbon-containing material pressurized thermochemical reaction unit through a carbon-poor particle sealing return device, and the axial included angle between the carbon-containing material pressurized thermochemical reaction unit and the lining pipeline and the carbon-poor particle sealing return device is 40-90 degrees respectively.

The lower part of the three-stage multiphase flow diverter is connected with the top inlet of the multiphase flow quenching settler, the inlet of the pumping quenching pipe is composed of a pumping throat sleeved in the reducing joint, an annular cavity is formed between the reducing joint and the pumping throat, the quenching agent enters the pumping quenching pipe from the reducing joint and is mixed with high-temperature gas-solid mixed fluid output by the three-stage multiphase flow diverter through the annular cavity, the pumping quenching pipe is positioned at 1/5-2/3 of the vertical height of the cone part of the three-stage multiphase flow diverter, and the included angle between the central line and the vertical line is 30-65 degrees.

The bottom of the multiphase flow quenching settler is provided with cross-shaped discharge ports, each discharge port is connected with a first cross processor and a second cross processor through a cut-off valve, and the outlets of the first cross processor and the second cross processor are combined and then connected with the inlet of the light distillate multi-effect recovery tower.

The diverter lining pipeline is connected with the secondary lining pipeline through a heat capacity coupling compensation regulator.

The method of the invention is as follows: a) The carbonaceous material firstly enters a carbonaceous material pretreatment device of a carbonaceous material feeding system) to prepare powder particles with the water content less than or equal to 4.0wt% and the particle size range of 100-1000 mu m, then enters a mixed material reinforced transfer area of a carbonaceous material pressurized thermochemical reaction unit after passing through a carbonaceous material conveying device and a material conveying control device connected with a conveying medium, and the produced high-temperature gas-solid mixed fluid after thermochemical conversion is sent into a first-stage multiphase flow diverter from a hydro-thermal cracking reaction area at the top of the carbonaceous material pressurized thermochemical reaction unit;

b) The carbon-lean particles with the carbon content of 1.00 to 10.00 weight percent, which are obtained by the diversion of the primary multiphase flow diverter, enter a fluidization dipleg of the primary multiphase flow diverter, are circulated back to a multiphase flow temperature regulation area at the middle lower part of the carbonaceous material pressurizing thermochemical reaction unit through a carbon-lean particle sealing material returning device, and high-temperature gas-solid mixed fluid output from the top of the primary multiphase flow diverter enters a secondary multiphase flow diverter through a lining pipeline;

c) The carbon-rich coarse particles with the particle size range being more than or equal to 50 mu m and the carbon content being 50.00-85.00 wt% captured by the secondary multiphase flow diverter enter a fluidization dipleg of the secondary multiphase flow diverter, the carbon-rich coarse particles are circularly returned to a circulating particle reinforced transfer area at the bottom of a carbon-rich particle chemical chain reaction unit through a carbon-rich coarse particle sealing material returning device, and high-temperature gas-solid mixed fluid output by the top of the secondary multiphase flow diverter enters the tertiary multiphase flow diverter through a lining pipeline;

d) The carbon-rich particles with the particle size ranging from 1 mu m to 50 mu m captured by the three-stage multiphase flow diverter enter a three-stage multiphase flow diverter fluidization dipleg, the carbon-rich particles flowing downwards in the three-stage multiphase flow diverter fluidization dipleg enter a graded slurry preparation unit after passing through a fluidization energy dissipater to be prepared into stable suspension, then the stable suspension is transferred into a suspension slurry storage tank, the suspension slurry enters a chemical chain initial reaction area in the middle of a carbon-rich particle chemical chain reaction unit through an active carbon-rich particle circulating and returning unit, and gas-solid mixed fluid output from the top of the three-stage multiphase flow diverter is mixed with quenching agent through a pumping quenching pipe and then enters a multiphase flow quenching settler;

e) The gas-liquid-solid mixed fluid entering a multiphase flow quenching settler is subjected to high-efficiency flow division, a gas phase product is output from the top of the multiphase flow quenching settler and enters the downstream for deep separation, the obtained liquid-solid mixed fluid enters a first cross processor and a second cross processor in a descending manner, then enters a light distillate oil multi-effect recovery tower after merging, finally enters a multiphase flow wet splitter for high-efficiency separation of multiphase flow, the heavy component obtained after flow division descends into a colloid particle splitter, the carbon-rich colloid particles obtained after separation enter a colloid particle modification activation tower for modification activation treatment, and the obtained porous active particles are circulated back to a mixed material strengthening transfer area at the lower part of a carbon-containing material pressurizing thermochemical reaction unit through a porous active particle conveyor;

f) The carbon-rich coarse particles which are circulated and returned to the bottom circulation particle reinforced transfer area of the carbon-rich particle chemical chain reaction unit through the carbon-rich coarse particle sealing material returning device are upwards moved through the carbon-rich particle activation area and are converged with the stable suspension which is fed into the chemical chain initial reaction area through the active carbon-rich fine particle circulating material returning unit in the step d), and then are upwards moved through the chemical chain deep reaction area and the transition regulation area in sequence, the high-temperature gas-solid mixed fluid which is generated after deep chemical chain conversion and contains the multi-attribute particles enters the multi-attribute particle shunt through the lining pipeline, and inert coarse particles which are obtained by shunting by the multi-attribute particle shunt downwards move into the fluidization dipleg of the multi-attribute particle shunt, and then are divided into two paths: one path is circulated back to the circulating particle reinforced transfer area at the bottom of the carbon-rich particle chemical chain reaction unit through a porous particle sealing material returning device), and the other path is circulated into the multiphase flow rectifying area of the carbon-containing material pressurizing thermochemical reaction unit through the heat capacity/bed density regulation and control fluidization circulating unit; inert coarse particles generated by the carbon-rich particle chemical chain reaction unit enter an inert particle discharge and heat energy recovery unit from a bottom outlet through a discharge lining pipeline;

g) The high-temperature gas-solid mixed fluid obtained by shunting through the multi-attribute particle shunt enters a multiphase flow rectifying area at the bottommost end of the carbonaceous material pressurizing thermochemical reaction unit through a lining pipeline, firstly flows into a multiphase flow temperature regulating area after being rectified with the multi-attribute particles from the heat capacity/bed density regulating and fluidizing circulating unit, then flows into a mixed material strengthening transfer area after being mixed with the carbon-lean particles from the carbon-lean particle sealing material returning device, finally flows into a hydro-thermal cracking reaction area for thermal cracking reaction after being mixed with qualified powder particles from a carbonaceous material feeding system, and thus the closed loop process cycle from step a) to step g) is completed.

The carbon-containing material is carbon-containing material with the volatile content of 20.00-45.00 wt%, the conveying medium (101) adopts one or more than two or circulating synthesis gas in fuel combustion flue gas with the CO ₂、N₂ and the oxygen content of less than or equal to 5.0vol%, the carbon-containing material steady-state conveying feedback device is connected with a mixed material strengthening transfer area of the carbon-containing material pressurizing thermochemical reaction unit, and an internal apparent flow rate of 20-50 m/s overheat protection steam is arranged at a carbon-containing material feeding port.

And (3) directly heating the heavy components output from the bottom of the multiphase flow wet flow divider to be more than or equal to 200 ℃ if the low-aromaticity intermediate phase with the volatile content of the colloidal particles being more than or equal to 40% by weight is obtained by the colloidal particles with the solid content of 40-60% by weight after entering the colloidal particle divider, and conveying the heavy components to a carbonaceous material pressurizing thermochemical reaction unit through a colloidal particle feeder for deep conversion.

The particle circulation factor of the multi-channel lean carbon circulation material returning system constructed by the carbon-containing material pressurizing thermochemical reaction unit, the primary multiphase flow diverter, the fluidization dipleg of the primary multiphase flow diverter and the lean carbon particle sealing material returning device is regulated and controlled within 50-300.

The activator enters a carbon-rich particle activation zone and a chemical chain initiation reaction zone of a carbon-rich particle chemical chain reaction unit respectively and then participates in thermochemical chain conversion reaction of carbonaceous materials, wherein the ratio of H ₂ O (g) partial pressure to O ₂ partial pressure [ (PH ₂O)/PO₂ ]. Gtoreq.1.0 ] in the activator entering the carbon-rich particle activation zone, and the ratio of H ₂ O (g) partial pressure to O ₂ partial pressure [ (PH ₂O)/PO₂ ]. Gtoreq.1.0 in the activator entering the chemical chain initiation reaction zone.

The inner diameters of different areas of the carbon-rich particle chemical chain reaction unit are marked as D1, D2 and D3, the height of the circulating particle reinforced transmission area at the lowest end is 0.5D1-1.5D1, the height of the carbon-rich particle activation area at the upper end of the circulating particle reinforced transmission area is 0.5D1-1.5D1, the height of the chemical chain initial reaction area at the upper end of the carbon-rich particle activation area is 0.05D2-D2, the height of the chemical chain depth reaction area at the upper end of the chemical chain initial reaction area is 0.5D2-4D 2, and the height of the transition control area at the topmost end is 0.5D3-2D 3.

The operation temperature of the carbon-rich particle chemical chain reaction unit is 950-1200 ℃, the operation pressure is 0.5-5 MPa, and the apparent speed of the internal mixed fluid is 0.8-5.0 m/s.

The operating temperature of the pressurizing thermochemical reaction unit for the carbonaceous material is 500-650 ℃, the operating pressure is 0.5-5 MPa, and the apparent speed of the internal mixed fluid is 0.8-5.0 m/s.

The operating temperature of the multiphase flow dry diversion unit is 480-630 ℃, and the operating pressure is 0.5-5 MPa.

The operating temperature of the multiphase flow quenching settler is 280-380 ℃ and the operating pressure is 0.5-5 MPa.

The operating temperature of the multiphase flow wet flow divider is 80-120 ℃ and the operating pressure is 0.1-0.5 MPa.

The invention adopts the efficient clean conversion and cascade utilization of different carbon-containing materials, can produce light oil products with high added value and high quality based on the core integrated process technology of the invention, and constructs a high-end energy chemical product synthetic chemical industry chain based on the deep processing of the light oil products and the conversion of synthesis gas.

The invention uses the carbonaceous materials such as petroleum coke, heavy oil sandstone, biomass, low-rank coal resources and the like as raw materials, can realize the efficient clean conversion and b-step utilization of the carbonaceous materials, is used for producing high-quality light oil products and synthesis gas, and can construct novel coal, oil, chemical and electricity poly-generation modes based on the cascade conversion device system of the carbonaceous materials.

Drawings

FIG. 1 is a schematic diagram of the overall structure of the present invention;

FIG. 2 is a flow chart of a pressurized thermochemical conversion system of the invention for carbonaceous material;

FIG. 3 is a schematic diagram of a carbon-rich particulate chemical chain reaction unit according to the present invention;

FIG. 4 is a schematic illustration of a pressurized thermochemical reaction unit of the carbonaceous material of the invention;

FIG. 5 is a schematic cross-sectional view of a draw quench tube of the present invention.

DETAILED DESCRIPTION OF EMBODIMENT (S) OF INVENTION

The system and method of the present invention will be described in further detail below with reference to the attached drawing figures.

The system comprises a carbonaceous material preparation system, a carbonaceous material pressurized thermochemical conversion system, a carbon-rich particle chemical chain conversion system and a multiphase flow diversion system;

Referring to fig. 1 and 2, the carbonaceous material preparation system comprises a carbonaceous material pretreatment sub-device 10, a carbonaceous material conveying device 11, a material conveying control device 12 and a carbonaceous material steady-state conveying feedback device 13 which are connected in sequence;

The multiphase flow diversion system comprises a multiphase flow dry diversion unit, a multiphase flow quenching settler 60 and a multiphase flow wet diversion 63;

The multiphase flow dry diversion unit comprises a multi-attribute particle diverter 22, a first-stage multiphase flow diverter 32, a second-stage multiphase flow diverter 40 and a third-stage multiphase flow diverter 50;

The carbonaceous material pressurized thermochemical conversion system comprises a carbonaceous material pressurized thermochemical reaction unit 30, a carbonaceous material feeding port 301 connected with a carbonaceous material steady-state conveying feedback device 13 and a porous active particle inlet 302 connected with a porous active particle returning unit 310 are respectively arranged on a mixed material enhanced transfer area 30-3 in the middle part of the carbonaceous material pressurized thermochemical reaction unit 30, an outlet of a multiphase flow rectifying area 30-1 at the bottom of the carbonaceous material pressurized thermochemical reaction unit 30 is connected with a heat capacity/bed density regulating fluidization circulation unit 27 through a refractory lining, the top of the carbonaceous material pressurized thermochemical reaction unit 30 is also connected with a first-stage multiphase flow diverter 32, lean carbon particles obtained by the diversion of the first-stage multiphase flow diverter 32 are sequentially connected with a multiphase flow temperature regulating area 30-2 of the carbonaceous material pressurized thermochemical reaction unit 30 through a first-stage multiphase flow diverter fluidization material leg 33 and a lean carbon particle sealing returning device 34, the high-temperature gas-solid mixed fluid output from the top of the first-stage multiphase flow diverter 32 enters the second-stage multiphase flow diverter 40 through the lining pipe 35, the carbon-rich coarse particles obtained by diversion of the second-stage multiphase flow diverter 40 flow downwards and circulate and return to the circulating particle reinforced transfer area 20-1 at the bottom of the carbon-rich particle chemical chain reaction unit 20 of the carbon-rich particle chemical chain conversion system sequentially through the fluidization dipleg 41 of the second-stage multiphase flow diverter and the carbon-rich coarse particle sealing return 42, the high-temperature gas-solid mixed fluid output from the top of the second-stage multiphase flow diverter 40 enters the third-stage multiphase flow diverter 50 through the second-stage lining pipe 43, the carbon-rich fine particles obtained by diversion of the third-stage multiphase flow diverter 50 flow downwards and sequentially enter the fluidization dipleg 51 of the third-stage multiphase flow diverter, the fluidized energy dissipater 52 enters a graded slurry preparation unit 53 connected with a compound slurry 104, a stable suspension is prepared and pumped into a suspension slurry storage tank 105, the suspension slurry storage tank 105 is connected with a chemical chain initiation reaction zone 20-3 of a carbon-rich particle chemical chain reaction unit 20 through an active carbon-rich fine particle circulating and returning unit 210, and a three-stage multiphase flow diverter 50 diverts the obtained gas-solid mixed fluid containing superfine particles to enter a multiphase flow quenching settler 60 of a multiphase flow separation system after being mixed with a quenching agent 103 in a pumping quenching pipe 54;

The carbon-rich particle chemical chain conversion system comprises a carbon-rich particle chemical chain reaction unit 20, an inert particle discharge pipe 25 is arranged at the outlet of the lower end of the carbon-rich particle chemical chain reaction unit 20, high-temperature inert particles discharged from the inert particle discharge pipe 25 travel into an inert particle discharge and heat energy recovery unit 80, the outlet of the upper end of the carbon-rich particle chemical chain reaction unit 20 is connected with a multi-attribute particle diverter 22 through a lining pipe 21, the upper end of the multi-attribute particle diverter 22 is connected with a multiphase rectification zone at the lower end of a carbonaceous material pressurizing thermochemical reaction unit 30 through a lining pipe 26, and the lower end of the multi-attribute particle diverter 22 is respectively connected with a porous particle sealing material returning device 24 and a heat capacity/bed density regulating fluidization circulation unit 27 through a multi-attribute particle diverter fluidization material leg 23;

The multiphase flow quenching settler 60 of the multiphase flow separation system is characterized in that the upper end of the multiphase flow quenching settler 60 is provided with a gas-phase product outlet 106, the lower end of the multiphase flow quenching settler 60 is respectively connected with inlets of a first cross processor 61a and a second cross processor 61b, the outlets of the first cross processor 61a and the second cross processor 61b are connected with the multiphase flow wet splitter 63 through a light distillate multi-effect recovery tower 62, heavy distillate separated by the multiphase flow wet splitter 63 is output by a heavy distillate outlet 107, heavy components obtained after splitting flow down enter a colloid particle splitter 64, carbon-rich colloid particles obtained after separating enter a colloid particle modification activation tower 65, porous active particles obtained by the colloid particle modification activation tower 65 are circularly returned to the carbonaceous material pressurizing thermochemical reaction unit 20 through a porous active particle conveyor 109, and an inlet connected with a modifier conveyor 108 is formed on the side wall of the colloid particle modification activation tower 65.

Referring to fig. 3, the carbon-rich particle chemical chain reaction unit 20 of the present invention includes a circulating particle reinforced transfer zone 20-1, a carbon-rich particle activation zone 20-2, a chemical chain initiation reaction zone 20-3, a chemical chain deep reaction zone 20-4 and a transition regulation zone 20-5 from bottom to top, and the side walls of the circulating particle reinforced transfer zone 20-1, the carbon-rich particle activation zone 20-2 and the chemical chain initiation reaction zone 20-3 are respectively provided with 1 to 10 activator inlets connected with an activator 200 through a flow control valve from bottom to top, and the suspension slurry storage tank 105 is connected with the chemical chain initiation reaction zone 20-3 of the carbon-rich particle chemical chain reaction unit 20 through an activated carbon-rich fine particle circulating return unit 210. The carbon-rich particle chemical chain reaction unit 20 is connected with the multi-attribute particle diverter 22 through the lining pipeline 21, the chemical leg 23 of the multi-attribute particle diverter 22 is connected with the inlet of the circulating particle reinforced transfer area 20-1 at the bottom of the connection of the carbon-rich particle chemical chain reaction unit 20 through the porous particle sealing return device 24, and the included angles between the central line of the carbon-rich particle chemical chain reaction unit 20 and the central lines of the porous particle sealing return device 24 and the carbon-rich particle sealing return device 42 are 40-90 degrees respectively.

Referring to fig. 4, the carbonaceous material pressurized thermochemical reaction unit 30 of the invention comprises a multiphase flow rectifying area 30-1, a multiphase flow temperature regulating area 30-2, a mixed material intensified transfer area 30-3 and a hydro-thermal cracking reaction area 30-4 from bottom to top, and a carbonaceous material inlet 301, a porous active particle sealed return unit 310 are communicated with the mixed material intensified transfer area 30-3, and the bottom of the multi-attribute particle diverter fluidization dipleg 23 is connected with the multiphase flow rectifying area 30-1 at the bottom of the carbonaceous material pressurized thermochemical reaction unit 30 through a heat capacity/bed density regulating fluidization circulation unit 27. The carbonaceous material pressurized thermochemical reaction unit 30 is connected with the primary multiphase flow diverter 32 through the lining pipeline 31 before, the material dissolving leg 33 of the primary multiphase flow diverter 32 is connected with the multiphase flow temperature regulating area 30-2 of the carbonaceous material pressurized thermochemical reaction unit 30 through the carbon-poor particle sealing return device 34, and the included angle between the central line of the carbonaceous material pressurized thermochemical reaction unit 30 and the central lines of the lining pipeline 31 and the carbon-poor particle sealing return device 34 is 40-90 degrees respectively.

Wherein the porous active particle returning unit 310 includes a colloidal particle diverter 64, a colloidal particle modification activation tower 65, and a modifier conveyor 108 and a porous active particle conveyor 109 connected to the colloidal particle modification activation tower 65.

Referring to fig. 5, the outlet end of the lower drawing quenching pipe 54 in the three-stage multiphase flow diverter 50 is connected with the inlet at the top of the multiphase flow quenching settler 60, the inlet end of the drawing quenching pipe 54 is composed of a drawing throat 54-2 sleeved with a reducing joint 54-1, an annular cavity 54-3 is formed between the reducing joint 54-1 and the drawing throat 54-2, the quenching agent 103 enters the drawing quenching pipe 54 from the reducing joint 54-1 and is mixed with the high-temperature gas-solid mixed fluid output by the three-stage multiphase flow diverter 50 through the annular cavity 54-3, the drawing quenching pipe 54 is positioned at 1/5-2/3 of the vertical height of the cone of the three-stage multiphase flow diverter 50, and the included angle between the center line and the vertical line is 30-65 degrees.

The bottom of the multiphase flow quenching settler 60 is provided with cross-shaped discharge ports, each discharge port is respectively connected with a first cross processor 61a and a second cross processor 61b through a cut-off valve, and the outlets of the first cross processor 61a and the second cross processor 61b are combined and then connected with the inlet of a light distillate oil multi-effect recovery tower 62.

Diverter lined conduit 26 is connected to secondary lined conduit 43 by a thermally coupled compensation regulator 70.

Referring to FIG. 1, the adaptive three-cycle pressurized carbonaceous material cascade conversion method of the invention comprises the steps of:

a) The carbonaceous material 100 firstly enters a carbonaceous material pretreatment device 10 of a carbonaceous material feeding system to prepare powder particles with the water content less than or equal to 4.0wt% and the particle size range of 100-1000 mu m, then enters a mixed material reinforced transfer area 30-3 of a carbonaceous material pressurized thermochemical reaction unit 30 after passing through a carbonaceous material conveying device 11 and a material conveying control device 12 connected with a conveying medium 102, and the produced high-temperature gas-solid mixed fluid after thermochemical conversion enters a first-stage multiphase flow diverter 32 from a hydro-thermal cracking reaction area 30-4 at the top of the carbonaceous material pressurized thermochemical reaction unit 30;

b) The carbon-lean particles with the carbon content of 1.00 to 10.00 weight percent, which are obtained by the diversion of the primary multiphase flow diverter 32, enter the primary multiphase flow diverter fluidization dipleg 33, are circularly returned to the multiphase flow temperature regulation and control area 30-2 at the middle lower part of the bottom of the carbonaceous material pressurized thermochemical reaction unit 30 through the carbon-lean particle sealing material returning device 34, and the high-temperature gas-solid mixed fluid output by the top end of the primary multiphase flow diverter 32 enters the secondary multiphase flow diverter 40 through the lining pipeline 35;

c) The carbon-rich coarse particles with the particle size range of more than or equal to 50 mu m and the carbon content of 50.00-85.00 wt% captured by the secondary multiphase flow diverter 40 enter a secondary multiphase flow diverter fluidization dipleg 41, the carbon-rich coarse particles are circulated and returned to a circulating particle reinforced transfer area 20-1 at the bottom of the carbon-rich particle chemical chain reaction unit 20 through a carbon-rich coarse particle sealing material returning device 42, and high-temperature gas-solid mixed fluid output by the top of the secondary multiphase flow diverter 40 enters a tertiary multiphase flow diverter 50 through a lining pipeline 43;

d) The carbon-rich fine particles with the particle size ranging from 1 mu m to 50 mu m captured by the three-stage multiphase flow diverter 50 enter a three-stage multiphase flow diverter fluidization dipleg 51, the carbon-rich particles flowing downwards in the three-stage multiphase flow diverter fluidization dipleg 51 enter a graded slurry preparation unit 53 after passing through a fluidization energy dissipater 52 to be prepared into stable suspension, then are transferred into a suspension slurry storage tank 105, enter a chemical chain initial reaction area 20-3 in the middle of a carbon-rich particle chemical chain reaction unit 20 through an active carbon-rich fine particle recycling and returning unit 210, and the gas-solid mixed fluid output from the top of the three-stage multiphase flow diverter 50 is mixed with a quenching agent 103 through a pumping quenching pipe 54 and then enters a multiphase flow quenching settler 60;

e) The gas-liquid-solid mixed fluid entering the multiphase flow quenching settler 60 is efficiently split, a gas phase product 106 is output from the top of the multiphase flow quenching settler 60 and enters the downstream for deep separation, the obtained liquid-solid multiphase product is divided into two flows which enter a first cross processor 61a and a second cross processor 61b and then enter a light distillate oil multi-effect recovery tower 62 after being converged, finally the obtained liquid-solid multiphase product enters a multiphase flow wet splitter 63 for efficient multiphase flow separation, the heavy component obtained after splitting is downward enters a colloid particle splitter 64, the separated carbon-rich colloid particles enter a colloid particle modification activation tower 65 for modification activation treatment, and the obtained porous active particles are circulated back to a mixed material strengthening transfer area 30-3 at the lower part of a carbonaceous material pressurizing thermochemical reaction unit through a porous active particle conveyor 109;

f) The carbon-rich particles which are circulated and returned to the circulating particle reinforced transfer area 20-1 at the bottom of the carbon-rich particle chemical chain reaction unit 20 through the carbon-rich particle sealing material returning device 42 are upwards moved through the carbon-rich particle activating area 20-2 and then are combined with the stable suspension 105 which enters the chemical chain starting reaction area 20-3 through the active carbon-rich fine particle circulating material returning unit 210 in the step d), and then are upwards moved through the chemical chain deep reaction area 20-4 and the transition regulation area 20-5 in sequence, the high-temperature gas-solid mixed fluid which is generated after deep chemical chain conversion and contains multi-attribute particles enters the multi-attribute particle diverter 22 through the lining pipeline 21, and inert coarse particles which are obtained by diversion of the multi-attribute particle diverter 22 are downwards moved into the multi-attribute particle diverter fluidization dipleg 23, and then are divided into two paths: one path of the circulating particles is circulated and returned to the circulating particle reinforced transfer area 20-1 at the bottom of the carbon-rich particle chemical chain reaction unit 20 through the porous particle sealing material returning device 24, and the other path of the circulating particles is conveyed to the multiphase flow rectifying area 30-1 of the carbon-containing material pressurizing thermochemical reaction unit 30 through the heat capacity/bed density regulating and controlling fluidization circulating unit 27; inert coarse particles generated by the carbon-rich particle chemical chain reaction unit 20 enter the inert particle discharging and heat energy recycling unit 80 from the bottom outlet through the discharging lining pipeline 25;

g) The high temperature gas-solid mixed fluid obtained by the diversion of the multi-attribute particle diverter 22 enters a multiphase flow rectifying area 30-1 at the bottommost end of a carbonaceous material pressurizing thermochemical reaction unit 30 through a lining pipeline 26, firstly flows into a multiphase flow temperature regulating area 30-2 after being rectified with the multi-attribute particles from a heat capacity/bed density regulating fluidization circulating unit 27, then flows into a mixed material strengthening transfer area 30-3 after being mixed with the carbon-lean particles from a carbon-lean particle sealing material returning device 34, finally flows into a hydro-thermal cracking reaction area 30-4 after being mixed with qualified powder particles from a carbonaceous material feeding system for thermal cracking reaction, and thus the closed loop process cycle from step a) to step g) is completed.

Wherein the carbonaceous material 100 is a carbonaceous material with the volatile content of 20.00-45.00 wt%, the conveying medium 102 adopts one or more than two or recycle synthesis gas in fuel combustion flue gas with the CO ₂、N₂ and the oxygen content of less than or equal to 5.0vol%, the carbonaceous material steady-state conveying feedback device 13 is connected with the mixed material strengthening transfer area 30-3 of the carbonaceous material pressurizing thermochemical reaction unit 30, and the carbonaceous material feeding port 301 is provided with overheat protection steam with the internal apparent flow rate of 20-50 m/s.

The heavy component output from the bottom of the multiphase flow wet process splitter 63 enters the colloid particle splitter 64, and if the colloid particles with the solid content of 40-60 wt% obtained are low-aromatic mesophase with the volatile content of more than or equal to 40wt%, the colloid particles can be directly heated to more than or equal to 200 ℃ without modification and activation and then conveyed to the carbonaceous material pressurized thermochemical reaction unit 30 for deep conversion.

The particle circulation factor of the multi-channel lean carbon circulation material returning system constructed by the carbonaceous material pressurizing thermochemical reaction unit 30, the first-stage multiphase flow diverter 32, the first-stage multiphase flow diverter fluidization dipleg 23 and the lean carbon particle sealing material returning device 34 can be regulated and controlled within the range of 50-300.

The activator enters a discharge lining pipeline 25 and a carbon-rich particle activation zone 20-2 and a chemical chain initiation reaction zone 20-3 of a carbon-rich particle chemical chain reaction unit 20 respectively to participate in the thermochemical chain conversion reaction of the carbonaceous material, wherein the ratio of H ₂ O (g) partial pressure to O ₂ partial pressure [ (P _H2O)/P_O2 ]. Gtoreq.1.0 ] in the activator entering the carbon-rich particle activation zone 20-2 and the ratio of H ₂ O (g) partial pressure to O ₂ partial pressure [ (P _H2O)/P_O2 ]. Gtoreq.1.0) in the activator entering the chemical chain initiation reaction zone 20-3;

The inner diameters of different areas of the carbon-rich particle chemical chain reaction unit 20 are denoted by D ₁,D₂ and D ₃, the circulating particle reinforced transfer area 20-1 is located in the range of 0.5D1-1.5D1 of the lowest height, the carbon-rich particle activation area 20-2 is located in the range of 0.5D1-1.5D1 of the upper height of the circulating particle reinforced transfer area 20-1, the chemical chain initiation reaction area 20-3 is located in the range of 0.05D ₂～D₂ of the upper height of the carbon-rich particle activation area 20-2, the chemical chain depth reaction area 20-4 is located in the range of 0.5D ₂～4D₂ of the upper height of the chemical chain initiation reaction area 20-3, and the transition control area is located in the range of 0.5D ₂～2D₃ of the highest height.

The operating temperature range of the carbon-rich particle chemical chain reaction unit (20) is 950-1200 ℃, the operating pressure is 0.5-5 MPa, and the apparent speed of the internal mixed fluid is 0.8-5.0 m/s.

The operating temperature range of the carbon-containing material pressurizing thermochemical reaction unit (30) is 500-650 ℃, the operating pressure is 0.5-5 MPa, and the apparent speed of the internal mixed fluid is 0.8-5.0 m/s.

The operating temperature range of the multiphase flow dry diversion system is 480-630 ℃, and the operating pressure range is 0.5-5 MPa.

The operating temperature range of the multiphase flow quenching settler 60 is 280-380 ℃ and the operating pressure is 0.5-5 MPa.

The operating temperature range of the multiphase flow wet splitter 63 is 80-120 ℃ and the operating pressure is 0.1-0.5 MPa.

The low-rank coal is subjected to the self-adaptive three-cycle pressurizing carbonaceous material cascade conversion device system and method disclosed by the invention, and the obtained medium-low temperature coal tar is subjected to dust removal, dehydration, desalination and purification in a subsequent coal tar pretreatment process, and then enters a fractionation and cutting system to cut the purified coal tar into light distillate, medium distillate and heavy distillate; the distillate oil with different distillation ranges is fed into a subsequent distillate oil deep conversion device system and finally converted into clean fuel oil with high added value, wherein the light distillate oil is extracted to obtain phenol products, dephenolized oil and middle distillate oil are fed into a fixed bed hydrogenation unit together, the heavy distillate oil is fed into a suspension bed hydrocracking unit for conversion, and the liquid products obtained by conversion are also fed into the fixed bed hydrogenation device system. The liquid products produced after the middle distillate and the heavy distillate are subjected to the hydrogenation of the suspension bed and the hydrogenation of the fixed bed enter a hydrogenation product separation and recovery device system, and finally, the LPG, the hydrogen and the liquid oiled products such as naphtha, diesel oil, wax oil, kerosene, high-octane gasoline and the like can be respectively obtained. The high hydrogen-carbon ratio synthetic gas generated by the device system can be used as raw material gas for synthesizing coal-based C1 chemical industry chains such as methanol, ethanol, SNG, F-T synthetic energy products and the like, and can also be used as fuel gas for IGCC clean fuel gas power generation.

Claims

1. The self-adaptive three-cycle pressurized carbonaceous material cascade conversion system is characterized by comprising a carbonaceous material preparation system, a carbonaceous material pressurized thermochemical conversion system, a carbon-rich particle chemical chain conversion system and a multiphase flow diversion system;

The carbonaceous material preparation system comprises a carbonaceous material pretreatment sub-device (10), a carbonaceous material conveying device (11), a material conveying control device (12) and a carbonaceous material steady-state conveying feedback device (13) which are sequentially connected;

The multiphase flow diversion system comprises a multiphase flow dry diversion unit, a multiphase flow quenching settler (60) and a multiphase flow wet diversion unit (63);

The multiphase flow dry diversion unit comprises a multi-attribute particle diverter (22), a primary multiphase flow diverter (32), a secondary multiphase flow diverter (40) and a tertiary multiphase flow diverter (50);

The carbonaceous material pressurized thermochemical conversion system comprises a carbonaceous material pressurized thermochemical reaction unit (30), a carbonaceous material feeding port (301) connected with a carbonaceous material steady-state conveying feedback device (13) and a porous active particle inlet (302) connected with a porous active particle returning unit (310) are respectively arranged on a mixed material enhanced transfer area (30-3) in the middle part of the carbonaceous material pressurized thermochemical reaction unit (30), an outlet of a multiphase flow rectifying area (30-1) at the bottom of the carbonaceous material pressurized thermochemical reaction unit (30) is connected with a heat capacity/bed density regulation fluidization circulating unit (27) through a refractory lining, the top of the carbonaceous material pressurized thermochemical reaction unit (30) is also connected with a first-stage multiphase flow diverter (32), lean carbon particles obtained by diversion of the first-stage multiphase flow diverter (32) sequentially pass through a first-stage multiphase flow diverter fluidization material leg (33), a lean carbon particle sealing feedback device (34) and a multiphase flow temperature regulation and control area (30-2) connected with the carbonaceous material pressurized thermochemical reaction unit (310), and high-temperature gas phase gas output at the top of the first-stage multiphase flow diverter (32) enters a second-stage multiphase flow diverter (40) through a second-stage multiphase flow diverter (41) to obtain coarse carbon particles which pass through the second-stage diverter (40) and flow separator (40) and the coarse carbon particles are sequentially discharged from the top of the carbonaceous material, the method comprises the steps that a carbon-rich coarse particle sealing material returning device (42) circularly returns to a circulating particle strengthening transfer area (20-1) at the bottom of a carbon-rich particle chemical chain reaction unit (20) of a carbon-rich particle chemical chain conversion system, high-temperature gas-solid mixed fluid output by the top of a secondary multiphase flow diverter (40) enters a tertiary multiphase flow diverter (50) through a secondary lining pipeline (43), carbon-rich fine particles obtained by diversion of the tertiary multiphase flow diverter (50) flow downwards and sequentially enter a tertiary multiphase flow diverter fluidization material leg (51) and a fluidization energy absorber (52) and then enter a graded slurry preparation unit (53) connected with a compound slurry (104), a stable suspension is prepared and then enters a suspension slurry storage tank (105), the suspension slurry (105) is connected with a chemical chain starting reaction area (20-3) of the carbon-rich particle chemical chain reaction unit (20) through an active carbon-rich fine particle circulating material returning unit (210), and the gas-solid mixed fluid containing superfine particles obtained by diversion of the tertiary multiphase flow diverter (50) enters a multi-phase quenching system (60) after being mixed with a quenching agent (103) in a pumping pipe (54);

The carbon-rich particle chemical chain conversion system comprises a carbon-rich particle chemical chain reaction unit (20), an inert particle discharge pipe (25) is arranged at the outlet of the lower end of the carbon-rich particle chemical chain reaction unit (20), high-temperature inert particles discharged through the inert particle discharge pipe (25) travel into an inert particle discharge and heat energy recovery unit (80), the outlet of the upper end of the carbon-rich particle chemical chain reaction unit (20) is connected with a multi-attribute particle diverter (22) through a lining pipeline (21), the upper end of the multi-attribute particle diverter (22) is connected with a multiphase rectification zone at the lower end of a carbonaceous material pressurizing thermochemical reaction unit (30) through a diverter lining pipeline (26), and the lower end of the multi-attribute particle diverter (22) is connected with a porous particle sealing material returning device (24) and a heat capacity/bed density regulating fluidization circulation unit (27) through a multi-attribute particle diverter fluidization material leg (23);

The multiphase flow quenching settler (60) of the multiphase flow separation system is characterized in that the upper end of the multiphase flow quenching settler (60) is provided with a gas-phase product outlet (106), the lower end of the multiphase flow quenching settler is respectively connected with inlets of a first cross processor (61 a) and a second cross processor (61 b), the outlets of the first cross processor (61 a) and the second cross processor (61 b) are connected with the multiphase flow wet splitter (63) through a light fraction oil multi-effect recovery tower (62), heavy fraction oil separated by the multiphase flow wet splitter (63) is output by a heavy fraction oil outlet (107), heavy components obtained after splitting flow downwards enter a colloid particle splitter (64), porous active particles obtained by separating the colloid particle modification activation tower (65) enter a colloid particle modification activation tower (65), and then enter a porous active particle thermochemical reaction unit (30) through a porous active particle conveyer, and an inlet connected with a modifier conveyer (108) is formed in the side wall of the colloid particle modification activation tower (65);

The carbon-rich particle chemical chain reaction unit (20) comprises a circulating particle reinforced transfer area (20-1), a carbon-rich particle activation area (20-2), a chemical chain initial reaction area (20-3), a chemical chain deep reaction area (20-4) and a transition regulation area (20-5) from bottom to top, wherein the side wall of the circulating particle reinforced transfer area (20-1), the side wall of the carbon-rich particle activation area (20-2) and the side wall of the chemical chain initial reaction area (20-3) are respectively provided with 1-10 activator inlets connected with an activator (200) through a flow control valve from bottom to top, and a suspension slurry storage tank (105) is connected with the chemical chain initial reaction area (20-3) of the carbon-rich particle chemical chain reaction unit (20) through an active carbon-rich fine particle circulating returning unit (210);

The carbonaceous material pressurizing thermochemical reaction unit (30) comprises a multiphase flow rectifying area (30-1), a multiphase flow temperature regulating area (30-2), a mixed material strengthening transfer area (30-3) and a hydro-thermal cracking reaction area (30-4) from bottom to top, a carbonaceous material inlet (301), a porous active particle sealing return unit (310) are communicated with the mixed material strengthening transfer area (30-3), and the bottom of the multi-attribute particle diverter fluidization dipleg (23) is connected with the multiphase flow rectifying area (30-1) at the bottom of the carbonaceous material pressurizing thermochemical reaction unit (30) through a heat capacity/bed density regulating fluidization circulation unit (27).

2. The adaptive three-cycle pressurized carbonaceous material cascade conversion system of claim 1, wherein the porous activated particle return unit (310) comprises a colloidal particle diverter (64), a colloidal particle modification activation tower (65), and a modifier conveyor (108) and a porous activated particle conveyor (109) coupled to the colloidal particle modification activation tower (65).

3. The self-adaptive three-cycle pressurized carbonaceous material cascade conversion system according to claim 1, wherein the carbon-rich particle chemical chain reaction unit (20) is connected with the multi-attribute particle diverter (22) through a lining pipeline (21), the multi-attribute particle diverter fluidization dipleg (23) is connected with an inlet of a circulating particle reinforced transfer area (20-1) at the bottom of the carbon-rich particle chemical chain reaction unit (20) through a porous particle sealing return device (24), and the axial included angles between the axial direction of the carbon-rich particle chemical chain reaction unit (20) and the axial direction of the porous particle sealing return device (24) and the axial included angles between the axial direction of the carbon-rich particle sealing return device (42) are respectively 40-90 degrees.

4. The self-adaptive three-cycle pressurized carbonaceous material cascade conversion system of claim 1, wherein the carbonaceous material pressurized thermochemical reaction unit (30) is connected with the primary multiphase flow diverter (32) through the lining pipe (31), the primary multiphase flow diverter fluidization dipleg (33) is connected with the multiphase flow temperature regulation area (30-2) of the carbonaceous material pressurized thermochemical reaction unit (30) through the carbon-depleted particle seal return (34), and the axial included angles of the carbonaceous material pressurized thermochemical reaction unit (30) and the lining pipe (31) and the carbon-depleted particle seal return (34) are respectively 40-90 degrees.

5. The self-adaptive three-cycle pressurized carbonaceous material cascade conversion system according to claim 1, wherein the outlet end of the lower pumping quench tube (54) of the three-stage multiphase flow diverter (50) is connected with the inlet at the top of the multiphase flow quenching settler (60), the inlet end of the pumping quench tube (54) is composed of a reducing joint (54-1) and a pumping throat (54-2) sleeved in the reducing joint, an annular cavity (54-3) is formed between the reducing joint (54-1) and the pumping throat (54-2), the quenching agent (103) enters the pumping quench tube (54) from the reducing joint (54-1) and is mixed with the high-temperature gas-solid mixed fluid output by the three-stage multiphase flow diverter (50) through the annular cavity (54-3), the pumping quench tube (54) is positioned at 1/5-2/3 of the vertical height of the conical part of the three-stage multiphase flow diverter (50), and the included angle between the center line and the vertical line is 30-65 degrees.

6. The self-adaptive three-cycle pressurized carbonaceous material cascade conversion system according to claim 1, wherein the bottom of the multiphase flow quenching settler (60) is provided with cross-shaped discharge ports, each discharge port is respectively connected with a first cross processor (61 a) and a second cross processor (61 b) through a cut-off valve, and the outlets of the first cross processor (61 a) and the second cross processor (61 b) are combined and then connected with the inlet of the light distillate oil multi-effect recovery tower (62).

7. The adaptive three-cycle pressurized carbonaceous material cascade conversion system of claim 1 wherein: the diverter lined pipe (26) is connected to the secondary lined pipe (43) by a thermal capacitance coupling compensation regulator (70).

8. The self-adaptive three-cycle pressurizing carbonaceous material step conversion method is characterized by mainly comprising the following steps of:

a) The method comprises the steps that a carbonaceous material (100) firstly enters a carbonaceous material pretreatment device (10) of a carbonaceous material feeding system to prepare powder particles with the water content less than or equal to 4.0wt% and the particle size range of 100-1000 mu m, then enters a mixed material strengthening transfer area (30-3) of a carbonaceous material pressurizing thermochemical reaction unit (30) after passing through a carbonaceous material conveying device (11) and a material conveying control device (12) connected with a conveying medium (101), and a high-temperature gas-solid mixed fluid generated after thermochemical conversion enters a first-stage multiphase flow divider (32) from a hydro-thermal cracking reaction area (30-4) at the top of the carbonaceous material pressurizing thermochemical reaction unit (30);

b) The carbon-lean particles with the carbon content of 1.00 to 10.00 weight percent, which are obtained by the diversion of the primary multiphase flow diverter (32), enter a fluidization dipleg (33) of the primary multiphase flow diverter, are circularly returned to a multiphase flow temperature regulation area (30-2) at the middle lower part of the carbonaceous material pressurizing thermochemical reaction unit (30) through a carbon-lean particle sealing material returning device (34), and high-temperature gas-solid mixed fluid output by the top of the primary multiphase flow diverter (32) enters a secondary multiphase flow diverter (40) through a lining pipeline (35);

c) The carbon-rich coarse particles with the particle size range being more than or equal to 50 mu m and the carbon content being 50.00-85.00 wt% captured by the secondary multiphase flow diverter (40) enter a secondary multiphase flow diverter fluidization dipleg (41), the carbon-rich coarse particles are circularly returned to a circulating particle reinforced transfer area (20-1) at the bottom of a carbon-rich particle chemical chain reaction unit (20) through a carbon-rich coarse particle sealing return device (42), and high-temperature gas-solid mixed fluid output by the top of the secondary multiphase flow diverter (40) enters a tertiary multiphase flow diverter (50) through a lining pipeline (43);

d) Carbon-rich fine particles with the particle size ranging from 1 mu m to 50 mu m captured by the three-stage multiphase flow diverter (50) enter a three-stage multiphase flow diverter fluidization dipleg (51), the carbon-rich particles flowing downwards in the three-stage multiphase flow diverter fluidization dipleg (51) enter a grading slurry preparation unit (53) after passing through a fluidization energy dissipater (52) to be prepared into stable suspension, then are transferred into a suspension slurry storage tank (105), enter a chemical chain initial reaction zone (20-3) in the middle of a carbon-rich particle chemical chain reaction unit (20) through an active carbon-rich fine particle circulation material returning unit (210), and gas-solid mixed fluid output from the top of the three-stage multiphase flow diverter (50) is mixed with a quenching agent (103) through a pumping quenching tube (54) and then enters a multiphase flow quenching settler (60);

e) The gas-liquid-solid mixed fluid entering a multiphase flow quenching settler (60) is subjected to high-efficiency split flow, a gas phase product (106) is output from the top of the multiphase flow quenching settler (60) and enters the downstream for deep separation, the obtained liquid-solid mixed fluid enters a first cross processor (61 a) and a second cross processor (61 b) in a downstream way, then enters a light distillate oil multi-effect recovery tower (62) after being converged, finally enters a multiphase flow wet splitter (63) for high-efficiency split flow, the heavy component obtained after split flow enters a colloid particle splitter (64), the separated carbon-rich colloid particles enter a colloid particle modification activation tower (65) for modification activation treatment, and the obtained porous active particles are recycled to a mixture material strengthening transfer area (30-3) at the lower part of a carbon-containing material pressurizing thermochemical reaction unit (30) through a porous active particle conveyor (109);

f) The carbon-rich coarse particles circularly returned to the carbon-rich particle chemical chain reaction unit (20) through the carbon-rich coarse particle sealing material returning device (42) are upwards moved through the carbon-rich particle activating region (20-2) and then are converged with the stable suspension liquid entering the chemical chain initial reaction region (20-3) through the active carbon-rich fine particle recycling material returning unit (210) in the step d), and then upwards moved through the chemical chain deep reaction region (20-4) and the transition regulation and control region (20-5) in sequence, the high-temperature gas-solid mixed fluid containing the multi-attribute particles generated after deep chemical chain conversion enters the multi-attribute particle diverter (22) through the lining pipeline (21), and the inert coarse particles obtained by diversion of the multi-attribute particle diverter (22) downwards move into the multi-attribute particle diverter fluidization material leg (23) and are divided into two paths: one path of the carbon-rich particles circularly returns to the circulating particle reinforced transfer area (20-1) at the bottom of the carbon-rich particle chemical chain reaction unit (20) through the porous particle sealing material returning device (24), and the other path of the carbon-rich particles passes through the heat capacity/bed density regulating and fluidizing circulating unit (27) to go into the multiphase flow rectifying area (30-1) of the carbonaceous material pressurizing thermochemical reaction unit (30); inert coarse particles generated by the carbon-rich particle chemical chain reaction unit (20) enter an inert particle discharge and heat energy recovery unit (80) from a bottom outlet through a discharge lining pipeline (25);

g) The high-temperature gas-solid mixed fluid obtained by diversion by the multi-attribute particle diverter (22) enters a multiphase flow rectifying area (30-1) at the bottommost end of a carbonaceous material pressurizing thermochemical reaction unit (30) through a diverter lining pipeline (26), firstly flows upwards into a multiphase flow temperature regulating area (30-2) after being rectified with the multi-particle from a heat capacity/bed density regulating fluidization circulating unit (27), then flows upwards into a mixed material strengthening transfer area (30-3) after being mixed with the carbon-lean particle from a carbon-lean particle sealing reversing device (34), finally flows into a hydro-thermal cracking reaction area (30-4) after being mixed with qualified powder particles from a carbonaceous material feeding system, and thus the closed loop process cycle from step a) to step g) is completed.

9. The self-adaptive three-cycle pressurized carbonaceous material cascade conversion method according to claim 8, wherein the carbonaceous material (100) is a carbonaceous material with a volatile content of 20.00-45.00 wt%, the conveying medium (101) is one or more than two or recycle synthesis gas of CO ₂、N₂ and fuel combustion flue gas with an oxygen content of less than or equal to 5.0vol%, the carbonaceous material steady-state conveying feedback device (13) is connected with a mixed material reinforced transfer area (30-3) of the carbonaceous material pressurized thermochemical reaction unit (30), and an internal apparent flow rate of 20-50 m/s overheat protection steam is arranged at the carbonaceous material feeding port (301).

10. The self-adaptive three-cycle pressurized carbonaceous material stepped conversion method according to claim 8, wherein heavy components output from the bottom of the multiphase flow wet process diverter (63) enter colloidal particles with solid content of 40-60 wt% obtained after the colloidal particles enter the colloidal particle diverter (64), and if volatile matters of the colloidal particles are low-aromatic mesophase with content of more than or equal to 40wt%, the colloidal particles are directly heated to more than or equal to 200 ℃, and then are conveyed to the carbonaceous material pressurized thermochemical reaction unit (30) through a colloidal particle feeder (310) for deep conversion.

11. The self-adaptive three-cycle pressurized carbonaceous material cascade conversion method of claim 8, wherein the particle circulation factor of the multi-channel lean carbon circulation and return system constructed by the carbonaceous material pressurized thermochemical reaction unit (30), the primary multiphase flow diverter (32), the primary multiphase flow diverter fluidization dipleg (33) and the lean carbon particle sealing return device (34) is regulated and controlled within 50-300.

12. The self-adaptive three-cycle pressurized carbonaceous material stepped conversion method according to claim 8, wherein the activator (200) enters a carbon-rich particle activation zone (20-2) of the discharge lining pipe (25) and the carbon-rich particle chemical chain reaction unit (20) respectively, and participates in the thermochemical chain conversion reaction of the carbonaceous material after entering the chemical chain initiation reaction zone (20-3), wherein the ratio of the partial pressure of H ₂ O (g) to the partial pressure of O ₂ in the activator entering the carbon-rich particle activation zone (20-2) is more than or equal to 1.0, and the ratio of the partial pressure of H ₂ O (g) to the partial pressure of O ₂ in the activator entering the chemical chain initiation reaction zone (20-3) is less than or equal to 1.0.

13. The self-adaptive three-cycle pressurized carbonaceous material cascade conversion method as claimed in claim 8, wherein the inside diameters of different areas of the carbon-rich particle chemical chain reaction unit (20) are numbered D1, D2 and D3, the circulating particle reinforced transfer area (20-1) is positioned at the lowest end height of 0.5D1-1.5D1, the carbon-rich particle activation area (20-2) is positioned at the upper end height of the circulating particle reinforced transfer area (20-1) of 0.5D1-1.5D1, the chemical chain initial reaction area (20-3) is positioned at the upper end height of 0.05D2-D2, the chemical chain depth reaction area (20-4) is positioned at the upper end height of the chemical chain initial reaction area (20-3) of 0.5D2-4D 2, and the transition control area (20-5) is positioned at the topmost height of 0.5D3-2D 3.

14. The method for stepwise converting a self-adaptive three-cycle pressurized carbonaceous material according to claim 8, wherein the carbon-rich particulate chemical chain reaction unit (20) is operated at a temperature of 950 to 1200 ℃, at a pressure of 0.5 to 5MPa, and at an apparent velocity of 0.8 to 5.0m/s.

15. The method for stepwise conversion of a self-adaptive three-cycle pressurized carbonaceous material of claim 8, wherein the pressurized thermochemical reaction unit (30) for the carbonaceous material operates at a temperature of between 500 and 650 ℃, at a pressure of between 0.5 and 5MPa, and at an apparent velocity of the internal mixed fluid of between 0.8 and 5.0m/s.

16. The method for stepwise converting a self-adaptive three-cycle pressurized carbonaceous material according to claim 8, wherein the multiphase flow dry diversion unit has an operating temperature of 480-630 ℃ and an operating pressure of 0.5-5 MPa.

17. The method for stepwise converting a self-adaptive three-cycle pressurized carbonaceous material according to claim 8, wherein the multiphase flow quenching settler (60) is operated at a temperature of 280 to 380 ℃ and at a pressure of 0.5 to 5MPa.

18. The method for stepwise converting a self-adaptive three-cycle pressurized carbonaceous material according to claim 8, wherein the multiphase flow wet splitter (63) has an operating temperature of 80 to 120 ℃ and an operating pressure of 0.1 to 0.5MPa.