CN111826204A - Up-down flow-dividing type oil-rich coal oil extraction co-production synthetic gas integrated device and method - Google Patents
Up-down flow-dividing type oil-rich coal oil extraction co-production synthetic gas integrated device and method Download PDFInfo
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- CN111826204A CN111826204A CN202010811020.2A CN202010811020A CN111826204A CN 111826204 A CN111826204 A CN 111826204A CN 202010811020 A CN202010811020 A CN 202010811020A CN 111826204 A CN111826204 A CN 111826204A
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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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- 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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- 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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- 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
- C10J3/72—Other features
- C10J3/721—Multistage gasification, e.g. plural parallel or serial gasification stages
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- 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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- 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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- 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
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- 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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- 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
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Abstract
The invention discloses an integrated device and a method for oil extraction and coproduction of synthesis gas of an up-and-down flow-dividing type oil-rich coal, 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 at most, and the 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 an integrated device and method for oil extraction and co-production of synthetic gas of vertically-divided rich oil coal.
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. CN205133505 discloses a polygeneration system for low-rank coal staged utilization, comprising a raw material coal pyrolysis and carbonization system and a entrained flow bed dry powder gasification system, wherein the pyrolysis and carbonization system carries out pyrolysis and carbonization treatment on high-water/high-ash low-rank coal to obtain raw coke gas, tar and semicoke, the raw coke gas is purified to obtain coal gas, the semicoke is gasified by an entrained flow bed, the low-rank coal pyrolysis and carbonization equipment controls the operation temperature to be 300 plus 550 ℃, and the internal temperature of the furnace is controlled by adopting self-heating or external heating operation, but the disclosed technology has the following technical defects: 1) the pyrolysis dry distillation reactor adopts raw material coal air drying base, the drying base volatile component of most raw material coal types reaches 48.14 percent, the tar yield is only 5 percent, the tar yield is very low, and the pyrolysis dry distillation reactor is limited by a process technology, and a large amount of coal tar is condensed into semicoke or cracked into raw coke gas components; 2) mixing a part of semicoke generated by pyrolysis of raw material coal with pulverized coal, then grinding the semicoke into powder again, and then gasifying the powder and the pulverized coal into a entrained-flow bed gasifier to prepare synthesis gas; 3) the coupling degree between the raw material coal pyrolysis and dry distillation system and the entrained flow bed dry powder gasification system is very low, and high-efficiency heat and material internal circulation are not established between the raw material coal pyrolysis and dry distillation system and the entrained flow bed dry powder gasification system; 4) the process flow is complex, the intensification degree among devices is low, the energy consumption of a process system is high, the energy efficiency level is low, and the technical economy competitiveness is not strong;
CN102504842A discloses a three-fluidized-bed solid heat carrier coal pyrolysis gasification combustion cascade utilization method, which comprises the step of mixing coal with high-temperature circulating ash in a circulating fluidized bed combustion furnace to generate pyrolysisAnd the semicoke which is not completely reacted in the fluidized bed gasification furnace is sent into a circulating fluidized bed combustion furnace to be burnt with oxygen-enriched gas, a solid heat carrier is heated, and the generated hot smoke gas is used for producing steam required by the gasification furnace. Although the method is adopted to realize the joint production of tar, pyrolysis gas and synthesis gas by decoupling pyrolysis, gasification and combustion and using high-temperature circulating ash as a solid heat carrier to carry out pyrolysis, gasification and combustion gradient utilization on coal, the existing problems are mainly as follows: partial pyrolysis semicoke is gasified, the remaining incompletely gasified semicoke is fed into a combustion furnace for oxygen-enriched gas combustion, and compared with the situation that the semicoke is completely gasified, the oxygen consumption is higher and a large amount of CO is generated2From the carbon balance point of view, the CO content of the whole process will be reduced, thus resulting in a reduction of the amount of effective synthesis gas of the whole process, i.e. the process specific oxygen consumption is high and the synthesis gas yield is low; in addition, according to the analysis of the whole process, semicoke which is not completely gasified is combusted in the circulating fluidized bed combustion furnace, and high-temperature circulating ash particles after combustion are finer, so that more fly ash in the synthetic gas generated after entering the fluidized bed gasification furnace can be caused, and the difficulty in subsequent dust removal of the synthetic gas can be increased.
Therefore, in order to overcome the bottleneck and challenge of the existing low-rank coal resource conversion technology at home and abroad, a novel integrated device and method for efficiently extracting oil from oil-rich coal and 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 an integrated device and a method for oil extraction and co-production of synthesis gas from oil-rich coal in an up-and-down flow-dividing manner, which can synchronously realize high-efficiency oil extraction of high-volatile oil-rich coal and high-efficiency conversion of active coke to co-produce high-quality hydrogen-rich synthesis gas.
In order to achieve the purpose, the invention adopts the following scheme:
an integrated device for oil extraction and coproduction of synthesis gas of an up-and-down flow-dividing type rich-oil coal comprises an active coke conversion furnace, a rich-oil 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 top outlet 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 bottom outlet of the gas-solid flow divider is connected with the inlet of the cooling buffer hopper through a fourth lining pipeline, the bottom outlet of the cooling buffer hopper is connected with the inlet of the lock hopper through a valve bank and a lining pipeline, the bottom outlet of the lock hopper is connected with a feeder through the valve bank and the lining pipeline, and the outlet of the feeder is connected with an inlet nozzle of the 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.
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 first reaction zone and a second reaction zone which are arranged from bottom to top, a cooling bed material interface is arranged between the cooling zone and the first 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 from the top of the cooling bed material interface 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 enters the second reaction zone under the action of an upward airflow to be mixed with oxygen and carry out secondary conversion.
Further, fine slag cooling agent is added into the fine slag cooling buffer to cool the fine slag, and the cooled fine slag is discharged to a fine slag sensible heat recovery system through a valve group 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 second lining pipeline and a gas-solid flow divider to 500-600 ℃ in advance;
(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 1300-1800 ℃ in a conversion temperature range, and the reaction temperature of the rich-oil coal thermal cracking reaction furnace is regulated to 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 ascends through the third lining pipeline and enters the gas-solid flow divider, and the inert fine particles enter the fine slag cooling buffer in a fluidized form through the second lining pipeline to recover sensible heat and then are discharged;
(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 through a fourth lining pipeline and enters a cooling buffer hopper;
(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 stream into a first reaction zone of the active coke converter through a middle feeding nozzle by a pneumatic conveying or mechanical feeding mechanism;
(8) the molten mass generated in the active coke converter descends into a cooling area, sensible heat recovery is realized under the action of a coarse slag coolant, coarse slag is finally discharged from a slag discharge port below, and the coarse slag enters a coarse 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 ascends to enter a second reaction zone and then is mixed with oxygen to carry out 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 continuously ascends through a first lining pipeline to enter a dispersion zone at the bottom of the rich-oil coal thermal cracking reaction furnace, and heat is provided for the thermal cracking reaction of fresh feed rich-oil coal after the rectification and temperature regulation of the mixed material flow.
Further, the initial temperature of the active coke stream entering the cooling buffer hopper is 450-800 ℃, the pressure is 0-9 MPaG, and 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; the starting material 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 system is 5-15 times of that of superheated steam, and a starting material transforming agent during system starting is air, oxygen-enriched air or pure oxygen.
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 gaseous oil-gas flow stream entering 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 of the core device of the up-down flow-dividing type oil-rich coal oil extraction co-production synthesis gas integrated device, the competitive advantages of all processes coupling, mild operation conditions and the like.
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 converter, 20-feeding nozzle oil-rich coal thermal cracking reactor, 30-gas-solid splitter, 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, 21-dispersion zone, 22-reaction zone, 23-separation zone, 24-bed layer interface, 101-start material, 102-start material converter, 103-oxygen, 104-oil-rich 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, 12-active coke cooling medium, 111-active coke transforming agent, 113-fine slag coolant, 114-coarse slag coolant, 115-oil gas coolant, 150-active coke particles, 151-feed stream, 152-start-up stream, 155-feed nozzle, 156-start-up nozzle, 11-cooling zone, 12-first reaction zone, 13-second reaction zone and 14-cooling bed material interface.
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, the integrated device for oil extraction and synthesis gas coproduction from rich-oil coal comprises a rich-oil coal thermal cracking reaction furnace 20, an active coke conversion furnace 10, a fine slag cooling buffer 70, a gas-solid flow divider 30, a cooling buffer hopper 40, a lock hopper 50 and a feeder 60.
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 bottom material inlet of the rich coal thermal cracking reaction furnace 20 is connected with the top outlet 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 the feeder 60 through a valve bank and a lining pipeline, and the outlet of the feeder 60 is connected with the inlet nozzle of the active coke conversion furnace 10.
The top outlet of the active coke conversion furnace 10 is connected with the bottom material inlet of the oil-rich coal thermal cracking reaction furnace 20 through a high-temperature resistant and wear resistant lining pipeline, and the bottom outlet of the active coke conversion furnace 10 is connected with a crude slag sensible heat recovery system 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 high-temperature resistant and wear resistant 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 through a valve bank and a lining pipeline.
The rich-oil 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 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 comprises a cooling zone 11, a first reaction zone 12 and a second 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 first 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 12 of the active coke conversion furnace 10 from the upper part of the cooling bed material interface 14 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 12, and a gas-solid mixed product carrying a small amount of fine molten mass enters the second reaction zone 13 under the action of an upward airflow to be mixed with oxygen and carry out secondary conversion. Under normal conditions, start-up nozzle 156 is a backup nozzle for feed stream 151.
The high-temperature-resistant and wear-resistant 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 refractory materials, namely a wear-resistant layer, a heat insulation layer and a heat preservation layer from inside to outside.
The fine slag cooling buffer 70 utilizes a fine slag coolant 113 to cool the fine slag, and then the fine slag is discharged to a fine slag sensible heat recovery system 108 through a valve bank and a lining pipeline, wherein 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 cooling buffer hopper 40, 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 is 450-800 ℃, and the pressure is 0-10 MPaG.
The operating pressure of the active coke conversion furnace 10 is 1-9 MPaG, the temperature of the cooling zone 11 is 180-300 ℃, the reaction temperature of the first reaction zone 12 is 1300-1800 ℃, and the reaction temperature of the second reaction zone 13 is 1-50 ℃ higher than that of the first reaction zone 12.
An integrated method for producing synthesis gas by oil extraction and coproduction of oil-rich coal in an up-and-down split flow manner 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 second lining pipeline 2 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 to feed, and 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 12 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 a 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 through the second lining pipeline 2 in a fluidized form to recover sensible heat and then are discharged;
(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 109 enters the feeder 60 through the lock hopper 50;
(7) the feeder 60 conveys the cooled active coke stream into the first reaction zone 12 of the active coke reformer 10 through a feeding nozzle by means of pneumatic conveying or mechanical feeding mechanism;
(8) the molten mass generated in the active coke converter 10 enters the cooling zone 11 downwards, sensible heat recovery is realized under the action of the coarse slag coolant 114, and the coarse slag is finally discharged from a slag discharge port at the lower part and enters a coarse 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 ascends to enter the second reaction zone 13 and then is mixed with oxygen to generate secondary conversion, so that the temperature of the second reaction zone 13 is 1-50 ℃ higher than that of the first reaction zone 12, the mixed material flow consisting of the crude synthesis gas and the high-temperature fine molten mass generated in the second reaction zone 13 continuously ascends through the first lining pipeline 1 to enter the dispersion zone 21 at the bottom of the rich-oil coal thermal cracking reaction furnace 20, and heat is provided for the thermal cracking reaction of fresh feed rich-oil coal after the rectification and temperature regulation of the mixed material flow.
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 starting material transforming agent 102 is prepared from air, oxygen-enriched air, pure oxygen and CO2And two or more of superheated steam, and air, oxygen-enriched air, pure oxygen or CO2The mass flow of the superheated steam 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 (10)
1. The utility model provides an upper and lower shunting 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);
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 third lining pipeline (3), the bottom material inlet of the rich coal thermal cracking reaction furnace (20) is connected with the top outlet of the active coke conversion furnace (10) through a 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 second lining pipeline (2);
the bottom outlet of the gas-solid flow divider (30) is connected with the inlet of the cooling buffer hopper (40) through a fourth lining pipeline (4), the bottom outlet 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 outlet of the lock hopper (50) is connected with the feeder (60) through the valve bank and the lining pipeline, and the outlet of the feeder (60) is connected with the inlet nozzle of the active coke conversion furnace (10);
the bottom outlet of the active coke conversion furnace (10) is connected with a sensible heat recovery system (107) of the coarse slag through a valve bank and a lining pipeline, and the bottom outlet of the fine slag cooling buffer (70) is connected with a sensible heat recovery system (108) of the fine slag.
2. The integrated device for oil extraction and synthesis gas coproduction of oil-rich coal with up-down split flow 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 device for oil extraction and synthesis gas coproduction of oil-rich coal with up-down split flow according to claim 1, characterized in that: the active coke conversion furnace (10) comprises a cooling zone (11), a first reaction zone (12) and a second 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 first reaction zone (12), a feed stream (151) consisting of active coke particles (150) and an active coke conversion agent (111) from a feeder (60), and a start-up stream (152) consisting of a start-up material (101) and a start-up material conversion agent (102) respectively enter the first reaction zone (12) of the active coke conversion furnace (10) from the top of the active coke conversion furnace (10) through a feed nozzle (155) and a start-up nozzle (156) above the cooling bed material interface (14), and gas-solid two-phase reaction is carried out in the first reaction zone (12), and a gas-solid mixed product carrying a small amount of fine molten mass enters the second reaction zone (13) under the action of the ascending gas flow to be mixed with oxygen and carry out secondary conversion. Under normal conditions, the start-up nozzle (156) is a backup nozzle for the feed stream (151).
4. The integrated device for producing synthesis gas by coal oil extraction with rich oil and by combining up and down flow dividing according to claim 1, 2 or 3, is characterized in that: the fine slag is cooled by adding a fine slag coolant (113) into the fine slag cooling buffer (70) and then discharged to 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.
5. The integrated device for producing synthesis gas by coal oil extraction with rich oil and by combining up and down flow dividing according to claim 1, 2 or 3, is 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.
6. An integrated method for oil-rich coal oil extraction and synthesis gas coproduction based on the up-and-down split 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 second lining pipeline (2) and a gas-solid flow divider (30) to 500-600 ℃ in advance;
(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 (12) of the active coke conversion furnace (10) is gradually increased to a 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 a feeding load;
(4) the mixture of oil gas and active coke generated in the rich coal thermal cracking reaction furnace (20) goes upward 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) through a second lining pipeline (2) in a fluidized form to recover sensible heat and then are discharged;
(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), feeding the cooled active coke stream (109) into a feeder (60) through a lock hopper (50);
(7) the feeder (60) conveys the cooled active coke stream into a first reaction zone (12) of the active coke converter (10) through a middle feeding nozzle by a pneumatic conveying or mechanical feeding mechanism;
(8) the molten mass generated in the active coke converter (10) flows downwards to enter a cooling area (11), sensible heat recovery is realized under the action of a coarse slag coolant (114), coarse slag is finally discharged from a slag discharge port below, and the coarse slag enters a coarse 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) ascends to enter a second reaction zone (13) and then is mixed with oxygen to carry out secondary conversion, so that the temperature of the second reaction zone (13) is 1-50 ℃ higher than that of the first reaction zone (12), the mixed material flow consisting of crude synthesis gas and high-temperature fine molten mass generated in the second reaction zone (13) continuously ascends to enter a dispersion zone (21) at the bottom of the rich-oil coal thermal cracking reaction furnace (20) through a first lining pipeline (1), and heat is provided for the thermal cracking reaction of fresh feed rich-oil coal after rectification and temperature regulation of the mixed material flow.
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 initial temperature of the active coke stream entering the cooling buffer hopper (40) is 450-800 ℃, the pressure is 0-9 MPaG, and the operating pressure of the active coke conversion furnace (10) is 1-10 MPaG.
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 starting material (101) is active coke, pulverized coal, heavy oil, diesel oil, natural gas, LNG, LPG or a mixture thereof; the starting material transforming agent (102) 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.
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 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.
10. 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; the gaseous oil and gas flow entering the oil and gas recovery system (106) passes through the middle CH4The 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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