CN111826205A - Down-flow parallel-flow type oil-rich coal oil extraction co-production synthetic gas integrated device and method - Google Patents
Down-flow parallel-flow type oil-rich coal oil extraction co-production synthetic gas integrated device and method Download PDFInfo
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- CN111826205A CN111826205A CN202010811025.5A CN202010811025A CN111826205A CN 111826205 A CN111826205 A CN 111826205A CN 202010811025 A CN202010811025 A CN 202010811025A CN 111826205 A CN111826205 A CN 111826205A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
- C10J3/60—Processes
- C10J3/64—Processes with decomposition of the distillation products
- C10J3/66—Processes with decomposition of the distillation products by introducing them into the gasification zone
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- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B49/00—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B49/00—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated
- C10B49/16—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with moving solid heat-carriers in divided form
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- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
- C10B53/04—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of powdered coal
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- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
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- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
- C10J3/721—Multistage gasification, e.g. plural parallel or serial gasification stages
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- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/093—Coal
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/0943—Coke
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0953—Gasifying agents
- C10J2300/0956—Air or oxygen enriched air
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0953—Gasifying agents
- C10J2300/0959—Oxygen
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- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0953—Gasifying agents
- C10J2300/0969—Carbon dioxide
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0953—Gasifying agents
- C10J2300/0973—Water
- C10J2300/0976—Water as steam
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Abstract
The invention discloses a descending parallel flow type oil-rich coal oil extraction co-production synthetic gas integrated device and a method, wherein the integrated device comprises an active coke conversion furnace, an oil-rich coal thermal cracking reaction furnace, a gas-solid flow divider, a cooling buffer hopper, a lock hopper, a feeder and a fine slag cooling buffer; the direct coupling of pulverized coal oil extraction and semicoke high-efficiency conversion is realized, the yield of tar can reach more than 20 percent, and high-quality hydrogen-rich synthesis gas is prepared by realizing the high-efficiency conversion of active coke in the same system; the technical defects of low utilization efficiency of coal resources, low comprehensive added value, low tar yield, poor quality of generated synthesis gas, serious pollution in the process and the like of the conventional low-rank coal pyrolysis and dry distillation process are overcome; the operation condition is mild, and the like, and can realize continuous, safe and stable operation.
Description
Technical Field
The invention belongs to the field of coal chemical industry, relates to a clean and efficient conversion and gradient utilization technology of low-rank coal, and particularly relates to a downward parallel flow type oil-rich coal oil extraction and synthesis gas coproduction integrated device and method.
Background
The 'energy gold triangle' areas where autonomous regions of Shanxi, Ningxia and inner Mongolia in the western region of China are located and the 'rich oil coal' resources in the autonomous region of Xinjiang are very rich, and according to prediction, the reserve and annual output of the precious 'rich oil coal' resources respectively account for more than 50% of the total reserve and annual output of the coal resources in China. 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 the 'oil-rich coal' resource at home and abroad and the existing low-rank coal resource conversion technology, a novel integrated device and method for efficiently extracting oil from oil-rich coal, efficiently converting active semicoke and co-producing high-quality hydrogen-rich synthetic gas are urgently needed to be developed.
Disclosure of Invention
The invention aims to provide a descending parallel flow type oil-rich coal oil extraction co-production synthesis gas integrated device and method, which can synchronously realize high-efficiency oil extraction of high-volatile oil-rich coal and high-efficiency active coke conversion to co-produce high-quality hydrogen-rich synthesis gas.
In order to achieve the purpose, the invention adopts the following scheme:
a downward parallel flow type oil-rich coal oil extraction co-production synthesis gas integrated device comprises an active coke conversion furnace, an oil-rich coal thermal cracking reaction furnace, a gas-solid flow divider, a cooling buffer hopper, a lock hopper, a feeder and a fine slag cooling buffer;
the top outlet of the rich coal thermal cracking reaction furnace is connected with the inlet of the gas-solid flow divider through a third lining pipeline, the bottom material inlet of the rich coal thermal cracking reaction furnace is connected with the high-temperature gas-solid mixed fluid outlet at the side of the active coke conversion furnace through a first lining pipeline, and the bottom outlet of the rich coal thermal cracking reaction furnace is connected with the inlet of the fine slag cooling buffer through a second lining pipeline;
the outlet at the bottom of the gas-solid flow divider is connected with the inlet of the cooling buffer hopper through a fourth lining pipeline;
an outlet at the bottom of the cooling buffer hopper is connected with an inlet of the lock hopper through a valve bank and a lining pipeline;
the outlet at the bottom of the lock hopper is connected with a feeder through a valve bank and a lining pipeline, and the outlet of the feeder is connected with an active coke inlet nozzle of an active coke converter;
the bottom outlet of the active coke converter is connected with a crude slag sensible heat recovery system through a valve bank and a lining pipeline; and the bottom outlet of the fine slag cooling buffer is connected with a fine slag sensible heat recovery system through a valve bank and a lining pipeline.
Furthermore, 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, a bed layer interface is arranged between the dispersion area and the reaction area, and oil-rich coal powder and inert particle bed materials enter the oil-rich coal thermal cracking reaction furnace from the lower part of the bed layer interface.
Further, the active coke converter comprises a cooling zone, a second reaction zone and a first reaction zone which are arranged from bottom to top, a cooling bed material interface is arranged between the cooling zone and the second reaction zone, a feed material flow consisting of active coke particles and an active coke conversion agent from a feeder and a start material flow consisting of a start material and a start material conversion agent respectively enter the first reaction zone of the active coke converter through a feed nozzle and a start nozzle at the top of the active coke converter, gas-solid two-phase reaction is carried out in the first reaction zone, and a gas-solid mixed product carrying a small amount of fine molten mass flows downwards by means of gravity to enter the second reaction zone to be mixed with oxygen and carry out secondary conversion.
Further, adding a fine slag coolant into the fine slag cooling buffer to cool the fine slag, and then feeding the cooled fine slag into a fine slag sensible heat recovery system through a valve bank and a lining pipeline, wherein the temperature of the fine slag output by the fine slag cooling buffer is 120-250 ℃, the pressure of the fine slag output by the fine slag cooling buffer is 0-10 MPaG, and the particle size range of the fine slag is 200-1000 mu m.
Furthermore, the first lining pipeline, the second lining pipeline, the third lining pipeline and the fourth lining pipeline are sequentially provided with three layers of refractory materials, namely a wear-resistant layer, a heat insulation layer and a heat preservation layer from inside to outside.
An integrated method for oil extraction and coproduction of synthesis gas from oil-rich coal comprises the following steps:
(1) adding inert particles into the oil-rich coal thermal cracking reaction furnace before the system is started and establishing bed material level;
(2) adjusting the composition and proportion of the starting material and the starting material conversion agent, and heating an active coke conversion furnace, a first lining pipeline, an oil-rich coal thermal cracking reaction furnace, a third lining pipeline and a gas-solid flow divider to a preset temperature of 500-600 ℃;
(3) after the system is heated to a preset temperature, the rich-oil coal thermal cracking reaction furnace starts feeding, and meanwhile, the composition and the proportion of the starting material and the starting material conversion agent are continuously adjusted, so that the reaction temperature of a first reaction zone of the active coke conversion furnace is gradually increased to a set conversion temperature range of 1300-1800 ℃, and the reaction temperature of the rich-oil coal thermal cracking reaction furnace is regulated to a set temperature of 450-800 ℃ through feeding load adjustment;
(4) the mixture of oil gas and active coke generated in the rich-oil coal thermal cracking reaction furnace flows upwards and enters a gas-solid flow divider through a third lining pipeline, and inert fine particles enter a fine slag cooling buffer in a fluidized form through a second lining pipeline to recover sensible heat and then are discharged to a fine slag sensible heat recovery system;
(5) after gas-solid separation is carried out on the gas-solid mixed fluid output from the top of the oil-rich coal thermal cracking reaction furnace in a gas-solid flow divider, the gaseous oil-gas flow stream is cooled by an oil-gas coolant and then flows upwards to enter an oil-gas recovery system, and the solid active coke flow stream flows downwards to enter a cooling buffer hopper through a fourth lining pipeline;
(6) after the active coke stream is subjected to sensible heat recovery in a cooling buffer hopper, the cooled active coke stream enters a feeder through a lock hopper;
(7) the feeder conveys the cooled active coke particles into a first reaction zone of the active coke converter through a top feeding nozzle by a pneumatic conveying or mechanical feeding mechanism;
(8) the crude molten mass generated in the active coke converter continuously enters a cooling area downwards under the action of flow guide, fluid dynamics and gravity in the equipment, sensible heat recovery is realized under the action of a crude slag coolant, crude slag is finally discharged from a slag discharge port below, and the crude slag enters a crude slag sensible heat recovery system through a valve bank and a pipeline;
(9) and the mixed material flow carrying a small amount of fine molten mass in the active coke conversion furnace flows downwards by virtue of gravity to enter a second reaction zone, then is mixed with oxygen and is subjected to secondary conversion, so that the temperature of the second reaction zone is 1-50 ℃ higher than that of the first reaction zone, the mixed material flow consisting of the crude synthesis gas and the high-temperature fine molten mass generated in the second reaction zone enters a dispersion zone at the bottom of the rich-oil coal thermal cracking reaction furnace from a high-temperature gas-solid mixed fluid outlet at the side of the active coke conversion furnace through a first lining pipeline, and heat is provided for the thermal cracking reaction of fresh feed rich-oil coal after multiphase fluid rectification and temperature regulation.
Further, the active coke cooling medium and the active coke stream are subjected to full heat exchange in a cooling buffer hopper and sensible heat is recovered, the initial temperature of the active coke stream is 450-800 ℃, and the pressure is 0-9 MPaG; the operating pressure of the active coke converter is 1-10 MPaG.
Further, the starting material is active coke, pulverized coal, heavy oil, diesel oil, natural gas, LNG, LPG or a mixture thereof, and the converting agent of the starting material is air, oxygen-enriched air or pure oxygen; the active coke transforming agent consists of air, oxygen-enriched air, pure oxygen and CO2Two or more of them and superheated steam, and air, oxygen-enriched air, pure oxygen or CO2The mass flow of the active coke is 5-15 times of that of superheated steam, and the active coke conversion agent is air, oxygen-enriched air or pure air during system startupOxygen.
Furthermore, the apparent space velocity in the oil-rich coal thermal cracking reaction furnace is 0.5-15 m/s, and the circulation rate of the inert particle bed material is 50-300 times.
Further, the oil-rich coal powder has 25-50 wt% of volatile matter, 5-15 wt% of ash and a feeding particle size range of 50-500 μm; CH in the crude oil-gas stream entering the oil-gas recovery system4The content of H is 0.05-1 vol%2The content of the carbon dioxide is 10-30 vol%, the content of CO is 30-65 vol%, and the content of tar gas is 15-30 vol%.
Compared with the prior art, the invention has the following beneficial effects and competitive advantages:
1) breaks through the conventional low-rank coal conversion technical route. 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 pulverized coal oil extraction and the efficient semicoke conversion is realized. The conventional coking process, the low-rank coal pyrolysis and the lump coal dry distillation process can obtain a small amount of coal tar and can also produce blocky semi-coke and semi-coke as byproducts, and the added values of the semi-coke and the semi-coke are lower, so that the direct coupling of the low-rank coal oil extraction and the high-efficiency conversion of the active coke is realized on the engineering level, the yield of tar can reach more than 20 percent at most, and the high-quality hydrogen-rich synthesis gas is prepared by the high-efficiency conversion of the active coke in the same system;
3) the device has stable and reliable performance. The low-rank coal pyrolysis technology at the present stage has the advantages of long process flow, complex equipment structure, low system integration degree, high device operation severity, incapability of realizing long-period, stable and safe operation, and continuous, safe and stable operation can be realized based on the unique structural design and competitive advantages of all processes coupling, mild operation conditions and the like of the core device of the downlink parallel flow type oil-rich coal oil extraction co-production synthesis gas integrated device.
4) The device has low operation cost. Compared with the conventional process technology, the brand-new oil-rich coal oil extraction co-production synthesis gas integrated device disclosed by the invention has the remarkable competitive advantages of low system operation severity, high system integration degree, high energy efficiency level, low investment intensity, low operation unit consumption and the like.
Drawings
FIG. 1 is a schematic view of the overall structure of the present invention
In the figure: 10-active coke conversion furnace, 20-rich oil coal thermal cracking reaction furnace, 30-gas-solid flow divider, 40-cooling buffer hopper, 50-lock hopper, 60-feeder, 70-fine slag cooling buffer, 1-first lining pipeline, 2-second lining pipeline, 3-third lining pipeline, 4-fourth lining pipeline, 11-cooling zone, 12-second reaction zone, 13-first reaction zone, 14-cooling bed material interface, 21-dispersing zone, 22-reaction zone, 23-separating zone, 24-bed layer interface, 101-start material, 102-start material conversion agent, 103-oxygen, 104-rich oil coal powder, 105-inert particle bed material, 106-oil gas recovery system, 107-coarse slag sensible heat recovery system, 108-fine slag sensible heat recovery system, 109-active coke stream, 111-active coke converting agent, 112-active coke cooling medium, 113-fine slag cooling agent, 114-coarse slag cooling agent, 115-oil gas cooling agent, 150-active coke particles, 151-feed stream, 152-start-up stream, 155-feed nozzle and 156-start-up nozzle.
Detailed Description
The present invention will be described in further detail with reference to the following examples, which are not intended to limit the invention thereto.
Referring to fig. 1, a down-flow parallel-flow oil-rich coal oil extraction co-production synthesis gas integrated device 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 lock hopper 50, a feeder 60 and a fine slag cooling buffer 70.
The top outlet of the rich coal thermal cracking reaction furnace 20 is connected with the inlet of the gas-solid flow divider 30 through a high-temperature resistant and wear-resistant third lining pipeline 3, the material inlet at the bottom of the rich coal thermal cracking reaction furnace 20 is connected with the high-temperature gas-solid mixed fluid outlet at the side of the active coke conversion furnace 10 through a high-temperature resistant and wear-resistant first lining pipeline 1, and the bottom outlet of the rich coal thermal cracking reaction furnace 20 is connected with the inlet of the fine slag cooling buffer 70 through a high-temperature resistant and wear-resistant second lining pipeline 2;
the bottom of the gas-solid flow divider 30 is connected with the inlet of the cooling buffer hopper 40 through a high-temperature-resistant and wear-resistant fourth lining pipeline 4;
the outlet at the bottom of the cooling buffer hopper 40 is connected with the inlet of the lock hopper 50 through a valve bank and a lining pipeline;
the bottom of the lock hopper 50 is connected with a feeder 60 through a valve bank and a lining pipeline, and the outlet of the feeder 60 is connected with an active coke inlet nozzle of the active coke converter 10;
a high-temperature gas-solid mixed fluid outlet on the side of the active coke reformer 10 is connected with a material inlet at the bottom of the rich coal thermal cracking reaction furnace 20 through a first lining pipeline 1, and a bottom outlet of the active coke reformer 10 is connected with a crude slag sensible heat recovery system 107 through a valve bank and a lining pipeline;
the top of the fine slag cooling buffer 70 is connected with the bottom outlet of the oil-rich coal thermal cracking reaction furnace 20 through a second lining pipeline 2, and the bottom outlet of the fine slag cooling buffer 70 is connected with a fine slag sensible heat recovery system 108 through a valve bank and a lining pipeline.
The rich-oil coal thermal cracking reaction furnace 20 is sequentially provided with a dispersion area 21, a reaction area 22 and a separation area 23 from bottom to top, a bed layer interface 24 is arranged between the dispersion area 21 and the reaction area 22, and the rich-oil coal powder material 104 and the inert particle bed material 105 enter the rich-oil coal thermal cracking reaction furnace 20 from the lower part of the bed layer interface 24.
The active coke conversion furnace 10 is divided into a cooling zone 11, a second reaction zone 12 and a first reaction zone 13 from bottom to top, a cooling bed material interface 14 between the cooling zone 11 and the second reaction zone 12, a feed material flow 151 consisting of active coke particles 150 and an active coke conversion agent 111 from a feeder 60, and a start material flow 152 consisting of a start material 101 and a start material conversion agent 102 enter the first reaction zone 13 of the active coke conversion furnace 10 through a feed nozzle 155 and a start nozzle 156 at the top of the active coke conversion furnace 10 respectively, gas-solid two-phase reaction is carried out in the first reaction zone 13, and a gas-solid mixed product carrying a small amount of fine melt descends to the second reaction zone 12 by virtue of gravity to be mixed with oxygen and undergo secondary conversion. Under normal conditions, start-up nozzle 156 is a backup feed nozzle for feed stream 151.
The first lining pipeline 1, the second lining pipeline 2, the third lining pipeline 3 and the fourth lining pipeline 4 are sequentially provided with three layers of wear-resistant, heat-insulating and heat-preserving refractory materials from inside to outside.
The fine slag cooling buffer 70 utilizes a fine slag coolant 113 to cool fine slag, and then the fine slag enters a fine slag sensible heat recovery system 108 through a valve bank and a lining pipeline, the temperature of the fine slag output by the fine slag cooling buffer 70 is 120-250 ℃, the pressure is 0-10 MPaG, and the particle size range is 200-1000 mu m.
The active coke cooling medium 112 and the active coke stream 109 perform sufficient heat exchange in the cooling buffer hopper 40 and recover sensible heat, the initial temperature of the active coke stream 109 is 450-800 ℃, and the pressure is 0-9 MPaG.
The operating pressure of the active coke conversion furnace 10 is 1-10 MPaG, the temperature of the cooling zone 11 is 180-300 ℃, the reaction temperature of the first reaction zone 13 is 1300-1800 ℃, and the reaction temperature of the second reaction zone 12 is 1-50 ℃ higher than that of the first reaction zone 13.
A downward parallel flow type oil-rich coal oil extraction co-production synthesis gas integrated method comprises the following steps:
(1) before the system is started, inert particles are added into the oil-rich coal thermal cracking reaction furnace 20 in advance and bed material level is established;
(2) the composition and the proportion of the start-up material 101 and the start-up material conversion agent 102 are adjusted through self-feedback, and the temperature of the active coke conversion furnace 10, the first lining pipeline 1, the rich coal thermal cracking reaction furnace 20, the third lining pipeline 3 and the gas-solid flow divider 30 is raised to a preset value of 500-600 ℃;
(3) after the system is heated to a preset temperature, the rich-oil coal thermal cracking reaction furnace 20 starts feeding, and meanwhile, the composition and the proportion of the active coke conversion furnace 10 and the active coke conversion agent 102 are continuously adjusted, so that the reaction temperature of the first reaction zone 13 of the active coke conversion furnace 10 is gradually increased to a set conversion temperature range of 1300-1800 ℃, and the reaction temperature of the rich-oil coal thermal cracking reaction furnace 20 is adjusted to a set temperature of 450-800 ℃ through adjustment of feeding load;
(4) the mixture of oil gas and active coke generated in the oil-rich coal thermal cracking reaction furnace 20 flows upwards into the third lining pipeline 3 and enters the gas-solid flow divider 30 through the third lining pipeline 3, and the inert fine particles enter the fine slag cooling buffer 70 in a fluidized form through the second lining pipeline 2 to recover sensible heat and then are discharged to the fine slag sensible heat recovery system 108;
(5) after gas-solid high-efficiency separation is carried out on the gas-solid mixed fluid output from the top of the rich coal thermal cracking reaction furnace 20 in the gas-solid flow divider 30, the gaseous oil-gas flow is cooled by the oil-gas coolant 115 and then flows upwards into the oil-gas recovery system 106, and the solid active coke flow 109 flows downwards and enters the cooling buffer hopper 40 through the fourth lining pipeline 4;
(6) after sensible heat recovery of the active coke stream 109 in the cooling buffer hopper 40, the cooled active coke stream 110 enters the feeder 60 through the lock hopper 50;
(7) the feeder 60 conveys the cooled active coke particles into the first reaction zone 13 of the active coke converter 10 through a feeding nozzle by a pneumatic conveying or mechanical feeding mechanism;
(8) the crude molten mass generated in the active coke converter 10 continuously enters the cooling area 11 in a descending manner under the action of flow guidance, fluid dynamics and gravity in the equipment, sensible heat recovery is realized under the action of a crude slag coolant, crude slag is finally discharged from a slag discharge port below, and the crude slag enters a crude slag sensible heat recovery system 107 through a valve bank and a pipeline;
(9) the mixed material flow carrying a small amount of fine molten mass in the active coke conversion furnace 10 flows downwards by means of gravity to enter a second reaction zone 12 and then is mixed with oxygen to carry out secondary conversion, so that the temperature of the second reaction zone 12 is 1-50 ℃ higher than that of a first reaction zone 13, the mixed material flow consisting of the raw synthesis gas and the high-temperature fine molten mass generated in the second reaction zone 12 enters a dispersion zone 21 at the bottom of the rich-oil coal thermal cracking reaction furnace 20 from a high-temperature gas-solid mixed fluid outlet at the side of the active coke conversion furnace 10 through a first lining pipeline 1, and heat is provided for the thermal cracking reaction of fresh feed rich-oil coal after multiphase fluid rectification and temperature regulation.
The starting material 101 can be gas fuel, solid fuel or mixed fuel such as active coke, pulverized coal, heavy oil, diesel oil, natural gas, LNG, LPG and the like, and the medium of the starting material transforming agent 102 during starting is air, oxygen-enriched air or pure oxygen.
The active coke transforming agent 111 is prepared from air, oxygen-enriched air, pure oxygen and CO2And two or more than two of superheated steam, and air, oxygen-enriched air, pure oxygen and CO in the active coke transforming agent 1112The mass flow is 5-15 times of that of the superheated steam.
The internal surface space velocity of the oil-rich coal thermal cracking reaction furnace 20 is 0.5-15 m/s, and the circulation rate of the inert particle bed material 105 is 50-300 times.
The oil-rich coal powder 104 comprises 25-50 wt% of volatile matter, 5-15 wt% of ash and 50-500 mu m of feeding particle size.
CH in the crude oil and gas stream entering the oil and gas recovery system 1064The content of H is 0.05-1 vol%2The content of the carbon dioxide is 10-30 vol%, the content of CO is 30-65 vol%, and the content of tar gas is 15-30 vol%.
Finally, it should be noted that: the above embodiments are only 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 to be covered by the claims.
Claims (9)
1. The utility model provides a down cocurrent flow formula rich oil coal carries oil coproduction synthetic gas integrated device which characterized in that: 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 lock hopper (50), a feeder (60) and a fine slag cooling buffer (70);
an outlet at the top of the rich oil coal thermal cracking reaction furnace (20) is connected with an inlet of the gas-solid flow divider (30) through a third lining pipeline (3), a material inlet at the bottom of the rich oil coal thermal cracking reaction furnace (20) is connected with a high-temperature gas-solid mixed fluid outlet at the side of the active coke conversion furnace (10) through a first lining pipeline (1), and an outlet at the bottom of the rich oil coal thermal cracking reaction furnace (20) is connected with an inlet of the fine slag cooling buffer (70) through a second lining pipeline (2);
the outlet at the bottom of the gas-solid flow divider (30) is connected with the inlet of the cooling buffer hopper (40) through a fourth lining pipeline (4);
an outlet at the bottom of the cooling buffer hopper (40) is connected with an inlet of the lock hopper (50) through a valve bank and a lining pipeline;
the outlet at the bottom of the lock hopper (50) is connected with a feeder (60) through a valve bank and a lining pipeline, and the outlet of the feeder (60) is connected with an active coke inlet nozzle of an active coke converter (10);
the bottom outlet of the active coke converter (10) is connected with a sensible heat recovery system (107) of the coarse slag through a valve bank and a lining pipeline; the bottom outlet of the fine slag cooling buffer (70) is connected with a fine slag sensible heat recovery system (108) through a valve bank and a lining pipeline.
2. The integrated downward parallel flow type oil-rich coal extraction and synthesis gas co-production device according to claim 1, characterized in that: the oil-rich coal thermal cracking reaction furnace (20) comprises a dispersion area (21), a reaction area (22) and a separation area (23) which are sequentially arranged from bottom to top, a bed layer interface (24) is arranged between the dispersion area (21) and the reaction area (22), and oil-rich coal powder (104) and inert particle bed materials (105) enter the oil-rich coal thermal cracking reaction furnace (20) from the lower part of the bed layer interface (24).
3. The integrated downward parallel flow type oil-rich coal extraction and synthesis gas co-production device according to claim 1, characterized in that: the active coke conversion furnace (10) comprises a cooling zone (11), a second reaction zone (12) and a first reaction zone (13) which are arranged from bottom to top, a cooling bed material interface (14) is arranged between the cooling zone (11) and the second reaction zone (12), a feed material flow (151) consisting of active coke particles (150) and an active coke conversion agent (111) from a feeder (60), and a start-up material flow (152) consisting of a start-up material (101) and a start-up material conversion agent (102) respectively enter the first reaction zone (13) of the active coke conversion furnace (10) through a feed nozzle (155) and a start-up nozzle (156) at the top of the active coke conversion furnace (10), and gas-solid two-phase reaction is carried out in the first reaction zone (13), and a gas-solid mixed product carrying a small amount of fine molten mass flows downwards to the second reaction zone (12) by virtue of gravity to be mixed with oxygen and subjected to secondary conversion.
4. The integrated downward parallel flow type oil-rich coal extraction and synthesis gas co-production device according to claim 1, characterized in that: the pipeline comprises a first lining pipeline (1), a second lining pipeline (2), a third lining pipeline (3) and a fourth lining pipeline (4), wherein three layers of refractory materials including a wear-resistant layer, a heat insulation layer and a heat preservation layer are sequentially arranged from inside to outside.
5. An integrated method for oil-rich coal oil extraction and synthesis gas coproduction based on the downstream parallel flow type integrated device for oil-rich coal oil extraction and synthesis gas coproduction as defined in any one of claims 1 to 5, which is characterized by comprising the following steps of:
(1) adding inert particles into the oil-rich coal thermal cracking reaction furnace (20) before the system is started and establishing bed material level;
(2) adjusting the composition and proportion of a starting material (101) and a starting material conversion agent (102), and heating an active coke conversion furnace (10), a first lining pipeline (1), an oil-rich coal thermal cracking reaction furnace (20), a third lining pipeline (3) and a gas-solid flow divider (30) to a preset temperature of 500-600 ℃;
(3) after the system is heated to a preset temperature, the rich-oil coal thermal cracking reaction furnace (20) starts to feed, meanwhile, the composition and the proportion of the starting material (101) and the starting material conversion agent (102) are continuously adjusted, so that the reaction temperature of the first reaction zone (13) of the active coke conversion furnace (10) is gradually increased to a set conversion temperature range of 1300-1800 ℃, and the reaction temperature of the rich-oil coal thermal cracking reaction furnace (20) is adjusted to a set temperature of 450-800 ℃ through adjustment of feeding load;
(4) the mixture of oil gas and active coke generated in the rich coal thermal cracking reaction furnace (20) flows upwards and enters a gas-solid flow divider (30) through a third lining pipeline (3), and inert fine particles enter a fine slag cooling buffer (70) in a fluidized form through a second lining pipeline (2) to recover sensible heat and then are discharged to a fine slag sensible heat recovery system (108);
(5) after gas-solid separation is carried out on gas-solid mixed fluid output from the top of the rich coal thermal cracking reaction furnace (20) in a gas-solid flow divider (30), a gaseous oil-gas flow stream is cooled by an oil-gas coolant (115) and then flows upwards to enter an oil-gas recovery system (106), and a solid active coke flow stream (109) flows downwards to enter a cooling buffer hopper (40) through a fourth lining pipeline (4);
(6) after sensible heat recovery of the active coke stream (109) in the cooling buffer hopper (40), the cooled active coke stream (110) enters a feeder (60) through a lock hopper (50);
(7) the feeder (60) conveys the cooled active coke particles into a first reaction zone (13) of the active coke converter (10) through a top feeding nozzle by a pneumatic conveying or mechanical feeding mechanism;
(8) the crude molten mass generated in the active coke converter (10) continuously flows downwards to enter a cooling area (11) under the action of flow guide, fluid dynamics and gravity in the equipment, sensible heat recovery is realized under the action of a crude slag coolant, and crude slag is finally discharged from a slag discharge port at the lower part, and enters a crude slag sensible heat recovery system (107) through a valve bank and a pipeline;
(9) the mixed material flow carrying a small amount of fine molten mass in the active coke conversion furnace (10) flows downwards by means of gravity to enter a second reaction zone (12) and then is mixed with oxygen to carry out secondary conversion, so that the temperature of the second reaction zone (12) is 1-50 ℃ higher than that of a first reaction zone (13), the mixed material flow consisting of crude synthesis gas and high-temperature fine molten mass generated in the second reaction zone (12) enters a dispersion zone (21) at the bottom of the rich-oil coal thermal cracking reaction furnace (20) through a high-temperature gas-solid mixed fluid outlet at the side of the active coke conversion furnace (10) through a first lining pipeline (1), and heat is provided for the thermal cracking reaction of fresh feed rich-oil coal after multiphase fluid rectification and temperature regulation.
6. The integrated method for oil extraction and synthesis gas coproduction of rich coal according to claim 6, wherein the method comprises the following steps: the active coke cooling medium (112) and the active coke stream (109) are subjected to sufficient heat exchange in a cooling buffer hopper (40) and sensible heat is recovered, the initial temperature of the active coke stream (109) is 450-800 ℃, and the pressure is 0-9 MPaG; the operating pressure of the active coke converter (10) is 1-10 MPaG.
7. The integrated method for oil extraction and synthesis gas coproduction of rich coal according to claim 6, wherein the method comprises the following steps: the starting material (101) is active coke, pulverized coal, heavy oil, diesel oil, natural gas, LNG, LPG or a mixture thereof, and the starting material transforming agent (102) is air, oxygen-enriched air or pure oxygen; the active coke transforming agent (111) is prepared from air, oxygen-enriched air, pure oxygen and CO2Two or more of them and superheated steam, and air, oxygen-enriched air, pure oxygen or CO2The mass flow of the system is 5-15 times of that of superheated steam, and the starting material transforming agent (102) is air, oxygen-enriched air or pure oxygen when the system is started.
8. The integrated method for oil extraction and synthesis gas coproduction of rich coal according to claim 6, wherein the method comprises the following steps: the internal surface space velocity of the oil-rich coal thermal cracking reaction furnace (20) is 0.5-15 m/s, and the circulation rate of the inert particle bed material (105) is 50-300 times.
9. The integrated method for oil extraction and synthesis gas coproduction of rich coal according to claim 6, wherein the method comprises the following steps: the oil-rich coal powder (104) comprises 25-50 wt% of volatile matter and 5-15 wt% of ash, and the particle size of the fed material is 50-500 mu m; CH in the crude oil and gas stream entering the oil and gas recovery system (106)4The content of H is 0.05-1 vol%2The content of the carbon dioxide is 10-30 vol%, the content of CO is 30-65 vol%, and the content of tar gas is 15-30 vol%.
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| CN113738336B (en) * | 2021-07-30 | 2022-06-07 | 西安交通大学 | Oil-rich coal underground pyrolysis heat energy cyclic utilization system |
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