CN212800244U - Chemical integrated system based on rich oil coal gas co-production technology - Google Patents
Chemical integrated system based on rich oil coal gas co-production technology Download PDFInfo
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Abstract
The utility model discloses a chemical integrated system based on rich oil coal oil gas co-production technology, which comprises a rich oil coal conversion system I, an oil-based chemical system II and a C1 chemical system III; performing thermal cracking on low-rank oil-rich coal by using an oil-rich coal conversion system I, an oil-based chemical system II and a C1 chemical system III to obtain hydrogen-rich synthetic gas, performing hydrocracking on products such as tar, semicoke and the like to prepare hydrogen, performing chemical processing on the obtained crude feed gas to obtain a DMC product, performing full product utilization on the low-rank oil-rich coal, realizing direct coupling of oil extraction of the low-rank coal and efficient conversion of active coke on an engineering layer, wherein the yield of the tar can reach more than 20 percent at most, and realizing efficient conversion of the active coke in the same system to prepare high-quality hydrogen-rich synthetic gas; the utility model has the advantages of the system integration degree is high, the efficiency level is high, investment intensity is low, the operation unit consumption is low.
Description
Technical Field
The utility model belongs to coal chemical industry field relates to clean high-efficient conversion of low order coal, step utilization technique, concretely relates to chemical integrated system based on rich oil coal oil gas coproduction technique.
Background
The 'rich oil coal' resource with high volatile content and high chemical reaction activity is a precious petroleum resource and has important significance for guaranteeing the energy strategic safety of China. How to realize the high-cost and high-value-added conversion of oil-rich coal resources, particularly more than 70 percent of pulverized coal resources generated in the conventional coal resource mining process, is the mainstream direction for the research and development of high-efficiency conversion technology of low-rank coal resources represented by oil-rich coal in China, wherein how to realize the high-efficiency conversion of active semicoke while realizing the high-efficiency oil extraction of the oil-rich coal through technical innovation, forms energy required by reaction between the oil-rich coal and the low-rank coal, and realizes the closed-loop balance and direct coupling of reaction materials, and is a technical problem which needs to be overcome urgently in the engineering development of high-energy efficiency and high-value-added conversion of the oil-rich coal resources.
Aiming at the bottleneck and challenge of the high-added-value conversion engineering technology development of 'rich oil coal' resources at home and abroad and the existing low-rank coal resource conversion technology, a novel chemical integrated process device system of a high-efficiency rich oil coal oil gas co-production technology is urgently needed to be developed.
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to provide a chemical integrated system based on rich oil coal oil gas coproduction technique has realized the direct coupling of low order coal oil extraction and active burnt high-efficient conversion to realize active burnt high-efficient conversion and prepare the rich hydrogen synthetic gas of high quality in same system.
In order to realize the purpose, the utility model adopts the following scheme:
a chemical integrated system based on rich oil coal oil gas co-production technology comprises a rich oil coal conversion system I, an oil-based chemical system II and a C1 chemical system III;
the oil-rich coal conversion system I comprises an active coke conversion furnace, an oil-rich coal thermal cracking reaction furnace, a gas-solid flow divider, a cooling buffer hopper, a powder storage bin, a feeder, an active coke conversion furnace fine slag cooling buffer and an oil-gas efficient separation device; converting the rich-oil coal into tar, heavy oil and hydrogen-rich synthesis gas by a rich-oil coal conversion system I;
the oil-based chemical system II comprises a feeding pretreatment device, a full-fraction hydrocracking device, a distillate oil hydrogenation upgrading device, a light fraction conversion device, a light hydrocarbon conversion device, a middle fraction conversion device and a heavy oil-light hydrocarbon coupling hydrogen production unit; in oil-based chemical systems II
Heavy oil, light hydrocarbon and distillate oil hydrogenation upgrading devices generated by the full-fraction hydrocracking device, a light fraction conversion device and light hydrocarbon generated by the light hydrocarbon conversion device are used as raw materials to prepare crude hydrogen in a heavy oil-light hydrocarbon coupling hydrogen production unit;
the first products output by the light fraction conversion device and the light hydrocarbon conversion device are C2-C4 low-carbon olefins;
a second product output by the middle distillate conversion device is mixed aromatic hydrocarbon mainly composed of BTX;
the crude hydrogen material flow generated and merged by the heavy oil hydrogen production device and the light hydrocarbon hydrogen production device of the heavy oil-light hydrocarbon coupling hydrogen production unit enters a hydrogen purification device for purification and purification until the purity is more than or equal to 95 percent, and then is used as a synthesis raw material of an oil-rich coal conversion system I and an oil-based chemical system II;
the C1 chemical system III comprises a raw material gas pretreatment unit and a hydrogen-carbon horizontal deviceA constant conversion unit, a raw material gas purification unit, a C1 chemical synthesis unit and CO2A separation and purification unit and a DMC synthesis unit; deep conversion processing is carried out on crude feed gas generated by a rich coal conversion system I in a C1 chemical system III to obtain DMC products, wherein hydrogen used is from an oil-based chemical system II.
Further, in the rich oil coal conversion system I, a material inlet at the bottom of the rich oil coal thermal cracking reaction furnace is connected with a high-temperature gas-solid mixed fluid outlet of the active coke conversion furnace through a valve bank and a lining pipeline, an outlet at the bottom of the rich oil coal thermal cracking reaction furnace is connected with an inlet of a fine slag cooling buffer through a valve bank and a lining pipeline, and an outlet at the bottom of the fine slag cooling buffer is connected with a fine slag sensible heat recovery system through a valve bank and a lining pipeline;
an outlet I at the top of the rich-oil coal thermal cracking reaction furnace is connected with an inlet of the oil-gas efficient separation device through a valve bank and a lining pipeline, an outlet II at the top of the rich-oil coal thermal cracking reaction furnace is connected with an inlet of a gas-solid flow divider through a lining pipeline, an outlet at the bottom of the gas-solid flow divider is connected with an inlet of a cooling buffer hopper through a lining pipeline, and a crude feed gas stream output from a gas phase outlet of the gas-solid flow divider is sent to an oil-based; the outlet at the bottom of the cooling buffer hopper is connected with the inlet of the powder storage bin through a valve bank and a lining pipeline, the outlet at the bottom of the powder storage bin is connected with a feeder through the valve bank and the lining pipeline, the outlet of the feeder is connected with an active coke inlet nozzle of an active coke converter, and the outlet at the bottom of the active coke converter is connected with a sensible heat recovery system of coarse slag through the valve bank and the lining pipeline.
Further, in the oil-based chemical system II, the feed pretreatment device is connected with an inlet of a full-cut hydrocracking device, a liquid phase outlet of the full-cut hydrocracking device is connected with an inlet of a distillate oil hydrogenation upgrading device, a light fraction outlet of the distillate oil hydrogenation upgrading device is connected with an inlet of a light fraction conversion device, a middle fraction outlet of the distillate oil hydrogenation upgrading device is connected with an inlet of the middle fraction conversion device, a light hydrocarbon outlet at the top of the full-cut hydrocracking device, a light hydrocarbon outlet at the top of the distillate oil hydrogenation upgrading device and a light hydrocarbon outlet at the top of the light fraction conversion device are converged through a pipeline and then divided into two branches, wherein a branch 1 is connected with the inlet of the light hydrocarbon conversion device, a branch 2 is connected with the inlet of the light hydrocarbon hydrogen production device, a heavy oil outlet at the bottom of the full-cut hydrocracking device is connected with the inlet of the heavy oil production device, a crude hydrogen outlet at the And the pure hydrogen stream output by the heavy oil-light hydrocarbon coupling hydrogen production unit is respectively connected with the inlet of the full-cut hydrocracking device, the inlet of the distillate oil hydrogenation upgrading device and the inlet of the raw material gas purification unit of the C1 chemical system III.
Furthermore, the heavy oil-light hydrocarbon coupling hydrogen production unit comprises a heavy oil hydrogen production device, a light hydrocarbon hydrogen production device and a hydrogen purification device.
Further, the light hydrocarbon hydrogen production device is a dry reforming hydrogen production device, a wet steam reforming hydrogen production device, an oxygen partial oxidation hydrogen production device or a mixed hydrogen production device.
Further, the full-range hydrocracking unit uses tar or heavy crude oil, atmospheric and vacuum residue, shale oil and thickened oil produced by a rich oil coal conversion system I; or one or more than two mixed raw materials in oil-coal slurry prepared by the heavy oil and the pulverized coal according to a proportion are used as the feeding materials.
Further, in the C1 chemical system III, the raw material gas stream from the rich coal conversion system I is connected to the inlet of the raw material gas pretreatment unit through a pipeline, the outlet of the raw material gas pretreatment unit is connected to the inlet of the hydrogen-carbon equilibrium conversion unit through a pipeline, the outlet of the hydrogen-carbon equilibrium conversion unit is connected to the inlet of the raw material gas purification unit through a pipeline, the bottom outlet of the raw material gas purification unit is connected to the inlet of the C1 chemical synthesis unit through a pipeline, the top outlet of the raw material gas purification unit is merged with the top outlet of the C1 chemical synthesis unit and then connected to CO through a pipeline2The inlets of the separation and purification units are connected, CO2The outlet of the separation and purification unit is connected with the inlet of the DMC synthesis unit through a pipeline, the bottom outlet of the C1 chemical synthesis unit is connected with a downstream deep processing system of the C1 chemical product through a pipeline, and the bottom outlet of the DMC synthesis unit is connected with a DMC product storage system through a pipeline.
Furthermore, the active coke conversion furnace takes active coke generated by the oil-rich coal thermal cracking reaction furnace as a raw material, and takes one or more than two mixed raw materials of pulverized coal, petroleum coke, biomass and shale which are prepared according to a proportion as a feeding material.
Further, the oil-rich coal thermal cracking reaction furnace comprises a dispersion area, a reaction area and a separation area which are sequentially arranged from bottom to top; the active coke conversion furnace comprises a cooling zone, a first reaction zone and a second reaction zone which are arranged from bottom to top. Further, the internal surface space velocity of the oil-rich coal thermal cracking reactor is 0.5-15 m/s, the circulation rate of the inert granular bed material is 50-300 times, the operating pressure is 1-10 MPaG, and the reaction temperature is 500-800 ℃; the operating pressure of the active coke conversion furnace is 1-10 MPaG, the temperature of the cooling zone is 180-300 ℃, the reaction temperature of the first reaction zone is 1300-1800 ℃, and the reaction temperature of the second reaction zone is 1-50 ℃ higher than that of the first reaction zone.
Compared with the prior art, the utility model discloses produced beneficial effect and competitive edge are:
1) breaks through the conventional low-rank coal conversion technical route. The utility model discloses an active coke reborner uses the active coke that rich oil coal thermal cracking reacting furnace produced as the raw materials among the rich oil coal conversion system I to the mixed raw materials that one or more than two kinds of proportion were prepared and are formed in fine coal, petroleum coke, living beings, shale is as the feeding. The technical defects that the conventional low-rank coal pyrolysis and dry distillation process has low utilization efficiency of coal resources, low comprehensive added value and low tar yield, lump coal and granular coal are generally used as raw materials, the quality of the generated synthesis gas is poor, the pollution in the process is serious and the like are overcome;
2) the direct coupling of the low-order pulverized coal oil extraction and the efficient semicoke conversion is realized. Conventional coking process, low order coal pyrolysis, lump coal dry distillation technology when obtaining a small amount of coal tar, still can the cubic blue charcoal of byproduct, semicoke usually, the blue charcoal of byproduct, the semicoke additional value is lower, the utility model discloses a rich oil coal conversion system I, oil base chemical industry system II, C1 chemical industry system III carry out the pyrolysis with the rich oil coal of low order and obtain rich hydrogen synthetic gas, products such as tar, semicoke carry out hydrocracking and prepare hydrogen, the crude feed gas that obtains carries out chemical processing and obtains the DMC product, carry out the full product utilization to the rich oil coal of low order, realized the direct coupling of low order coal oil extraction and active coke high-efficient conversion on the engineering layer, the tar yield can reach more than 20% at most to realize the high-quality rich hydrogen synthetic gas of preparing of active coke high-efficient conversion in same system.
3) The device has stable and reliable performance. The hot, dry distillation technique of low order coal at present stage all has that process flow is long, equipment structure is complicated, the system integration degree is low, the device operation severity is high, can't realize long period, stable, safe operation, based on a unique structural design and all competitive advantages such as the first technological process coupling of rich oil coal oil extraction coproduction synthetic gas integrated device core equipment of upper and lower shunting, operating condition are mild, can realize continuous, safe and stable operation.
4) The device has low operation cost. Compare conventional process technology, the utility model discloses a brand-new high-efficient oil gas coproduction of low order coal and the integrated system of the high added value chemical products of degree of depth conversion production have that the system operation severity is low, the system integrates the degree height, the efficiency level is high, investment intensity is low, the operation unit consumes low grade apparent competitive advantage.
Drawings
FIG. 1 is the utility model discloses a chemical industry integrated system schematic diagram based on rich oil coal oil gas coproduction technique
In the figure: 10-an active coke conversion furnace, 20-an oil-rich coal thermal cracking reaction furnace, 30-a gas-solid flow divider, 40-a cooling buffer hopper, 50-a powder storage bin, 60-a feeder, 70-a fine slag cooling buffer and 80-an oil-gas efficient separation device; 300-feed pretreatment unit, 400-full fraction hydrocracking unit, 500-distillate oil hydrogenation upgrading unit, 600-light fraction conversion unit, 610-light hydrocarbon conversion unit, 620-product I, 630-product II, 650-middle fraction conversion unit, 700-crude raw material gas pretreatment unit, 701-crude raw material gas stream, 710-hydrogen-carbon equilibrium conversion unit, 720-raw material gas purification unit, 730-C1 chemical synthesis unit, 740-CO2Separation and purification unit, 750-DMC synthesis unit, 760-C1 chemical product downstream deep processing system, 770-DMC product storage system, 800-heavy oil-light oilA hydrocarbon coupling hydrogen production unit, a 810-heavy oil hydrogen production device, an 820-light hydrocarbon hydrogen production device, an 830-hydrogen purification device, 850-crude hydrogen material flow, 860-first purified hydrogen material flow, 870-second purified hydrogen material flow, 21-material inlet at the bottom of the rich coal thermal cracking reaction furnace, 22-first outlet at the top of the rich coal thermal cracking reaction furnace, 23-a second outlet at the top of the rich-oil coal thermal cracking reaction furnace, 24-a bottom outlet of the rich-oil coal thermal cracking reaction furnace, an outlet of a 11-active coke converter high-temperature gas-solid mixed fluid, an inlet nozzle of 12-active coke converter active coke, an inlet of a 71-fine slag cooling buffer, an outlet at the bottom of a 72-fine slag cooling buffer, a 108-fine slag sensible heat recovery system, an inlet of a 31-gas-solid splitter and a 107-coarse slag sensible heat recovery system.
Detailed Description
The present invention will be described in further detail with reference to the following specific examples, which should not be construed as limiting the invention.
Referring to fig. 1, a chemical integrated system based on rich oil coal oil gas co-production technology comprises a rich oil coal conversion system I, an oil-based chemical system II, and a C1 chemical system III;
the rich-oil coal conversion system I comprises an active coke conversion furnace 10, a rich-oil coal thermal cracking reaction furnace 20, a gas-solid flow divider 30, a cooling buffer hopper 40, a powder storage bin 50, a feeder 60, an active coke conversion furnace fine slag cooling buffer 70 and an oil-gas efficient separation device 80.
The material inlet 21 at the bottom of the rich-oil coal thermal cracking reaction furnace is connected with the high-temperature gas-solid mixed fluid outlet 11 of the active coke conversion furnace through a valve bank and a lining pipeline, the outlet 24 at the bottom of the rich-oil coal thermal cracking reaction furnace is connected with the inlet 71 of the fine slag cooling buffer through a valve bank and a lining pipeline, and the outlet 72 at the bottom of the fine slag cooling buffer is connected with the sensible heat recovery system 108 of the fine slag through a valve bank and a lining pipeline.
An outlet I22 at the top of the rich-oil coal thermal cracking reaction furnace is connected with an inlet of the oil-gas efficient separation device 80 through a valve bank and a lining pipeline, an outlet II 23 at the top of the rich-oil coal thermal cracking reaction furnace is connected with an inlet 31 of a gas-solid flow divider through a lining pipeline, an outlet at the bottom of the gas-solid flow divider 30 is connected with an inlet of a cooling buffer hopper 40 through a lining pipeline, and a crude feed gas stream 701 output from a gas phase outlet of the gas-solid flow divider 30 is sent to an oil-based chemical; the outlet at the bottom of the cooling buffer hopper 40 is connected with the inlet of the powder storage bin 50 through a valve bank and a lining pipeline, the outlet at the bottom of the powder storage bin 50 is connected with the feeder 60 through a valve bank and a lining pipeline, the outlet of the feeder 60 is connected with the active coke inlet nozzle 12 of the active coke converter, and the outlet at the bottom of the active coke converter 10 is connected with the sensible heat recovery system 107 of the coarse slag through a valve bank and a lining pipeline.
The active coke conversion furnace 10 can use the active coke generated by the oil-rich coal thermal cracking reaction furnace 20 as one or more than two of the raw materials, the coal powder, the petroleum coke, the biomass, the shale and other carbon-rich raw materials which are prepared in proportion as the feeding material.
The oil-based chemical system II comprises a feed pretreatment device 300, a full-range hydrocracking device 400, a distillate oil hydrogenation upgrading device 500, a light fraction conversion device 600, a light hydrocarbon conversion device 610, a middle-range conversion device 650 and a heavy oil-light hydrocarbon coupling hydrogen production unit 800. The heavy oil-light hydrocarbon coupled hydrogen production unit 800 comprises a heavy oil hydrogen production device 810, a light hydrocarbon hydrogen production device 820 and a hydrogen purification device 830.
The full-range hydrocracking unit 400 takes one or more than two mixed raw materials in the tar, the heavy crude oil, the atmospheric and vacuum residue oil, the shale oil, the thick oil and the oil-coal slurry produced by the rich oil-coal conversion system I as the feed material. The feed pretreatment device 300 is connected with an inlet of the full-fraction hydrocracking device 400, a liquid phase outlet of the full-fraction hydrocracking device 400 is connected with an inlet of the distillate oil hydrogenation upgrading device 500, a light fraction outlet of the distillate oil hydrogenation upgrading device 500 is connected with an inlet of the light fraction conversion device 600, a middle fraction outlet of the distillate oil hydrogenation upgrading device 500 is connected with an inlet of the middle fraction conversion device 650, a light hydrocarbon outlet at the top of the full-fraction hydrocracking device 400, a light hydrocarbon outlet at the top of the distillate oil hydrogenation upgrading device 500 and a light hydrocarbon outlet at the top of the light fraction conversion device 600 are converged through a pipeline and then divided into two branches, wherein a branch 1 is connected with an inlet of the light hydrocarbon conversion device 610, a branch 2 is connected with an inlet of the light hydrocarbon hydrogen production device 820, a heavy oil outlet at the bottom of the full-fraction hydrocracking device 400 is connected with an inlet of the heavy oil hydrogen production device 810, a crude hydrogen outlet at the The inlet of the device 830 is connected, the purified hydrogen material flow output by the heavy oil-light hydrocarbon coupling hydrogen production unit 800 is divided into two branches, wherein the second purified hydrogen material flow 870 is connected with the inlet of the full fraction hydrocracking unit 400 and the inlet of the distillate oil hydrogenation upgrading device 500, and the first purified hydrogen material flow 860 is connected with the inlet of the raw material gas purification unit 720 of the C1 chemical system III.
The C1 chemical system III comprises a raw material gas pretreatment unit 700, a hydrogen-carbon balance conversion unit 710, a raw material gas purification unit 720, a C1 chemical synthesis unit 730, and CO2Separation and purification unit 740, DMC synthesis unit 750.
The crude raw material gas flow 701 is connected with an inlet of a crude raw material gas pretreatment unit 700 through a pipeline, an outlet of the crude raw material gas pretreatment unit 700 is connected with an inlet of a hydrogen-carbon balance conversion unit 710 through a pipeline, an outlet of the hydrogen-carbon balance conversion unit 710 is connected with an inlet of a raw material gas purification unit 720 through a pipeline, a bottom outlet of the raw material gas purification unit 720 is connected with an inlet of a C1 chemical synthesis unit 730 through a pipeline, a top outlet of the raw material gas purification unit 720 is converged with a top outlet of the C1 chemical synthesis unit 730 and then is connected with a CO through a pipeline2The inlets of the separation and purification units 740 are connected, and CO is2The outlet of the separation and purification unit 740 is connected with the inlet of a DMC (dimethyl carbonate) synthesis unit 750 through a pipeline, the outlet of the bottom of the C1 chemical synthesis unit 730 is connected with a C1 chemical product downstream deep processing system 760 through a pipeline, and the outlet of the bottom of the DMC synthesis unit 750 is connected with a DMC product storage system 770 through a pipeline.
The oil-rich coal thermal cracking reaction furnace 20 comprises a dispersion area, a reaction area and a separation area which are arranged from bottom to top in sequence.
The active coke conversion furnace 10 comprises a cooling zone, a first reaction zone, a second reaction zone and a cooling zone which are arranged from bottom to top.
The light hydrocarbon hydrogen production device 820 can be used for dry reforming hydrogen production, wet steam reforming hydrogen production, oxygen partial oxidation hydrogen production or mixed hydrogen production.
The internal surface space velocity of the reactor of the oil-rich coal thermal cracking reaction furnace 20 is 0.5-15 m/s, the circulation rate of the inert particle bed material 105 is 50-300 times, the operating pressure is 1-10 MPaG, and the reaction temperature is 500-800 ℃.
The operating pressure of the active coke conversion furnace 10 is 1-10 MPaG, the temperature of the cooling zone is 180-300 ℃, the reaction temperature of the first reaction zone is 1300-1800 ℃, and the reaction temperature of the second reaction zone is 1-50 ℃ higher than that of the first reaction zone.
Finally, it should be noted that: the above embodiments are only used for illustrating the technical solutions of the present invention and not for limiting the same, and although the present invention is described in detail with reference to the above embodiments, those of ordinary skill in the art should understand that: modifications and equivalents may be made to the embodiments of the invention without departing from the spirit and scope of the invention, which is intended to be covered by the claims.
Claims (10)
1. The utility model provides a chemical industry integrated system based on rich oil coal gas coproduction technique which characterized in that: the system comprises a rich coal conversion system I, an oil-based chemical system II and a C1 chemical system III;
the oil-rich coal conversion system I comprises an active coke conversion furnace (10), an oil-rich coal thermal cracking reaction furnace (20), a gas-solid flow divider (30), a cooling buffer hopper (40), a powder storage bin (50), a feeder (60), an active coke conversion furnace fine slag cooling buffer (70) and an oil-gas efficient separation device (80); converting the rich-oil coal into tar, heavy oil and hydrogen-rich synthesis gas by a rich-oil coal conversion system I;
the oil-based chemical system II comprises a feed pretreatment device (300), a full-range hydrocracking device (400), a distillate oil hydrogenation upgrading device (500), a light fraction conversion device (600), a light hydrocarbon conversion device (610), a middle-range conversion device (650) and a heavy oil-light hydrocarbon coupling hydrogen production unit (800); in an oil-based chemical system II, light hydrocarbons generated by a full-range hydrocracking device (400) and a distillate oil hydrogenation upgrading device (500), a light-range conversion device (600) and light hydrocarbons generated by a light-range conversion device (610) are used as raw materials to prepare crude hydrogen in a heavy-light hydrocarbon coupling hydrogen production unit (800);
the first product (620) output by the light fraction conversion device (600) and the light hydrocarbon conversion device (610) is C2-C4 low-carbon olefin;
a product II (630) output by the middle distillate conversion device (650) is mixed aromatic hydrocarbon with BTX as a main component;
the crude hydrogen stream (850) generated and merged by the heavy oil hydrogen production device (810) and the light hydrocarbon hydrogen production device (820) of the heavy oil-light hydrocarbon coupling hydrogen production unit (800) enters a hydrogen purification device (830) for purification until the purity is more than or equal to 95 percent, and then is used as a synthesis raw material of a rich oil coal conversion system I and an oil-based chemical system II;
the C1 chemical system III comprises a raw material gas pretreatment unit (700), a hydrogen-carbon equilibrium conversion unit (710), a raw material gas purification unit (720), a C1 chemical synthesis unit (730), and a CO2A separation and purification unit (740) and a DMC synthesis unit (750); deep conversion processing is carried out on crude feed gas generated by a rich coal conversion system I in a C1 chemical system III to obtain DMC products, wherein hydrogen used is from an oil-based chemical system II.
2. The chemical integrated system based on the rich oil coal gas co-production technology of claim 1, characterized in that: in the rich-oil coal conversion system I, a material inlet (21) at the bottom of a rich-oil coal thermal cracking reaction furnace is connected with a high-temperature gas-solid mixed fluid outlet (11) of an active coke conversion furnace through a valve bank and a lining pipeline, a bottom outlet (24) of the rich-oil coal thermal cracking reaction furnace is connected with an inlet (71) of a fine slag cooling buffer through the valve bank and the lining pipeline, and a bottom outlet (72) of the fine slag cooling buffer is connected with a fine slag sensible heat recovery system (108) through the valve bank and the lining pipeline;
a first outlet (22) at the top of the rich-oil coal thermal cracking reaction furnace is connected with an inlet of an oil-gas efficient separation device (80) through a valve bank and a lining pipeline, a second outlet (23) at the top of the rich-oil coal thermal cracking reaction furnace is connected with an inlet (31) of a gas-solid flow divider through a lining pipeline, an outlet at the bottom of the gas-solid flow divider (30) is connected with an inlet of a cooling buffer hopper (40) through a lining pipeline, and a crude feed gas stream (701) output from a gas phase outlet of the gas-solid flow divider (30) is sent to an oil-based; the outlet at the bottom of the cooling buffer hopper (40) is connected with the inlet of the powder storage bin (50) through a valve bank and a lining pipeline, the outlet at the bottom of the powder storage bin (50) is connected with the feeder (60) through the valve bank and the lining pipeline, the outlet of the feeder (60) is connected with an active coke inlet nozzle (12) of the active coke converter, and the outlet at the bottom of the active coke converter (10) is connected with a sensible heat recovery system (107) of the coarse slag through the valve bank and the lining pipeline.
3. The chemical integrated system based on the rich oil coal gas co-production technology of claim 1, characterized in that: in the oil-based chemical system II, a feed pretreatment device (300) is connected with an inlet of a full-fraction hydrocracking device (400), a liquid phase outlet of the full-fraction hydrocracking device (400) is connected with an inlet of a distillate oil hydrogenation upgrading device (500), a light fraction outlet of the distillate oil hydrogenation upgrading device (500) is connected with an inlet of a light fraction conversion device (600), a middle fraction outlet of the distillate oil hydrogenation upgrading device (500) is connected with an inlet of a middle fraction conversion device (650), a light hydrocarbon outlet at the top of the full-fraction hydrocracking device (400), a light hydrocarbon outlet at the top of the distillate oil hydrogenation upgrading device (500) and a light hydrocarbon outlet at the top of the light fraction conversion device (600) are converged through a pipeline and then divided into two branches, wherein the branch 1 is connected with an inlet of the light hydrocarbon conversion device (610), the branch 2 is connected with an inlet of a light hydrocarbon hydrogen production device (820), the heavy oil outlet at the bottom of the full-fraction hydrocracking device (400) is connected with the inlet of the heavy oil hydrogen production device (810), the crude hydrogen outlet at the top of the heavy oil hydrogen production device (810) is converged with the outlet at the top of the light hydrocarbon hydrogen production device (820) and then connected with the inlet of the hydrogen purification device (830), the purified hydrogen stream output by the heavy oil-light hydrocarbon coupling hydrogen production unit (800) is divided into two branches, wherein the second purified hydrogen stream (870) is connected with the inlet of the full-fraction hydrocracking device (400) and the inlet of the distillate oil hydrogenation upgrading device (500), and the first purified hydrogen stream (860) is connected with the inlet of the raw material gas purification unit (720) of the C1 chemical system III.
4. The chemical integrated system based on the rich oil coal gas co-production technology of claim 3, characterized in that: the heavy oil-light hydrocarbon coupling hydrogen production unit (800) comprises a heavy oil hydrogen production device (810), a light hydrocarbon hydrogen production device (820) and a hydrogen purification device (830).
5. The chemical integrated system based on the rich oil coal gas co-production technology of claim 4, characterized in that: the light hydrocarbon hydrogen production device (820) is a dry reforming hydrogen production device, a wet steam reforming hydrogen production device, an oxygen partial oxidation hydrogen production device or a mixed hydrogen production device.
6. The chemical integrated system based on the rich oil coal gas co-production technology of claim 3, or characterized in that: the full-range hydrocracking device (400) takes one or more than two mixed raw materials in oil-coal slurry prepared by the heavy oil and the pulverized coal as the feed according to the proportion, wherein the mixed raw materials are tar heavy crude oil, atmospheric and vacuum residue oil, shale oil and thickened oil produced by the rich oil-coal conversion system I.
7. The chemical integrated system based on the rich oil coal gas co-production technology of claim 1, characterized in that: in the C1 chemical system III, a crude raw material gas flow (701) from an oil-rich coal conversion system I is connected with an inlet of a crude raw material gas pretreatment unit (700) through a pipeline, an outlet of the crude raw material gas pretreatment unit (700) is connected with an inlet of a hydrogen-carbon equilibrium conversion unit (710) through a pipeline, an outlet of the hydrogen-carbon equilibrium conversion unit (710) is connected with an inlet of a raw material gas purification unit (720) through a pipeline, a bottom outlet of the raw material gas purification unit (720) is connected with an inlet of a C1 chemical synthesis unit (730) through a pipeline, a top outlet of the raw material gas purification unit (720) is converged with a top outlet of the C1 chemical synthesis unit (730) and then is connected with a CO through a pipeline2The inlets of the separation and purification units (740) are connected, and CO2The outlet of the separation and purification unit (740) is connected with the inlet of the DMC synthesis unit (750) through a pipeline, the bottom outlet of the C1 chemical synthesis unit (730) is connected with the deep processing system (760) downstream of the C1 chemical product through a pipeline, and the bottom outlet of the DMC synthesis unit (750) is connected with the DMC product storage system (770) through a pipeline.
8. The chemical integrated system based on the rich oil coal gas co-production technology of any one of claims 1-7, wherein: the active coke conversion furnace (10) takes active coke generated by the oil-rich coal thermal cracking reaction furnace (20) as a raw material, and takes one or more than two mixed raw materials of pulverized coal, petroleum coke, biomass and shale which are prepared according to a proportion as a feeding material.
9. The chemical integrated system based on the rich oil coal gas co-production technology of any one of claims 1-7, wherein: the oil-rich coal thermal cracking reaction furnace (20) comprises a dispersion area, a reaction area and a separation area which are sequentially arranged from bottom to top; the active coke conversion furnace (10) comprises a cooling zone, a first reaction zone and a second reaction zone which are arranged from bottom to top.
10. The chemical integrated system based on the rich oil coal gas co-production technology of any one of claims 1-7, wherein: the internal surface space velocity of the reactor of the oil-rich coal thermal cracking reaction furnace (20) is 0.5-15 m/s, the circulation rate of the inert particle bed material (105) is 50-300 times, the operating pressure is 1-10 MPaG, and the reaction temperature is 500-800 ℃; the operating pressure of the active coke conversion furnace (10) is 1-10 MPaG, the temperature of the cooling zone is 180-300 ℃, the reaction temperature of the first reaction zone is 1300-1800 ℃, and the reaction temperature of the second reaction zone is 1-50 ℃ higher than that of the first reaction zone.
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