CN117866663A - Fixed bed gasification system and fixed bed gasification method - Google Patents
Fixed bed gasification system and fixed bed gasification method Download PDFInfo
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- CN117866663A CN117866663A CN202410222652.3A CN202410222652A CN117866663A CN 117866663 A CN117866663 A CN 117866663A CN 202410222652 A CN202410222652 A CN 202410222652A CN 117866663 A CN117866663 A CN 117866663A
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- 238000002309 gasification Methods 0.000 title claims abstract description 156
- 238000000034 method Methods 0.000 title claims abstract description 51
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- 239000002893 slag Substances 0.000 claims abstract description 43
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 191
- 238000005406 washing Methods 0.000 claims description 98
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 74
- 238000000926 separation method Methods 0.000 claims description 71
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- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 claims description 29
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- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 16
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- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 1
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Classifications
-
- 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
- C10J3/02—Fixed-bed gasification of lump fuel
- C10J3/20—Apparatus; Plants
-
- 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
- C10J3/02—Fixed-bed gasification of lump fuel
-
- 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
-
- 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
- C10J3/82—Gas withdrawal means
- C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/002—Removal of contaminants
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/02—Dust removal
- C10K1/026—Dust removal by centrifugal forces
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
-
- 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
- C10J2300/0916—Biomass
-
- 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
- C10J2300/093—Coal
-
- 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
- C10J2300/0946—Waste, e.g. MSW, tires, glass, tar sand, peat, paper, lignite, oil shale
-
- 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
-
- 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
- C10J2300/0969—Carbon dioxide
-
- 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
-
- 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
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
- C10J2300/1603—Integration of gasification processes with another plant or parts within the plant with gas treatment
-
- 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
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
- C10J2300/1603—Integration of gasification processes with another plant or parts within the plant with gas treatment
- C10J2300/1615—Stripping
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Industrial Gases (AREA)
Abstract
The invention provides a fixed bed gasification system, which comprises a fixed bed gasification furnace, a scrubber and an oil scrubber; the fixed bed gasifier comprises a carbonaceous raw material inlet, a gasifying agent inlet, a crude product gas outlet and an ash outlet, and the gasifying agent inlet is communicated to a furnace core in the fixed bed gasifier; the scrubber comprises a crude product gas inlet, a first wash oil inlet and an oil-gas mixture outlet, and the crude product gas inlet is connected to the crude product gas outlet of the fixed bed gasifier; the oil scrubber comprises an oil-gas mixture inlet, a second wash oil inlet, a gas outlet and a dust-laden oil outlet, and its oil-gas mixture inlet is connected to the oil-gas mixture outlet of the scrubber. Also provided is a fixed bed gasification method, which is carried out by using the fixed bed gasification system. The invention has at least one of the following effects: the product gas has good dust removal and purification effects; the energy utilization rate is high; the sewage discharge amount is small; the sewage is easy to treat; the blockage is not easy to occur; the slag is simply discharged; the safety performance is good.
Description
Technical Field
The invention belongs to the technical field of fixed bed gasification, and particularly relates to a fixed bed gasification system and a fixed bed gasification method.
Background
The fixed bed gasifier is a gasifier fed with bulk raw materials, wherein the bulk raw materials in the fixed bed gasifier enter from the upper part and are in countercurrent contact with gasifying agents entering from the lower part to react, so that crude product gas and residual unreacted ash are generated. The crude product gas generally flows out from the upper part of the fixed bed gasifier, and oil, phenol, ammonia and other substances generated by thermal decomposition of the raw materials remain in the crude product gas because the crude product gas does not pass through a high-temperature section at the lower part of the gasifier, and in addition, the crude product gas also carries solid particles such as dust. The industrial water chilling mode is generally adopted to wash and cool the crude product gas, oil, phenol, ammonia and dust in the crude product gas are captured by water, and the formed wastewater can meet the requirements of biochemical water treatment after step-by-step deoiling, phenol recovery and ammonia recovery, so that the wastewater treatment difficulty is high and the cost is high.
Disclosure of Invention
A first object of the present invention is to provide a fixed bed gasification system capable of gasifying a carbonaceous feedstock and separating and purifying a produced raw product gas, which solves at least one of the problems of the prior art, and reduces the amount of wastewater produced.
A second object of the present invention is to provide a fixed bed gasification method for gasifying a carbonaceous feedstock by using the aforementioned fixed bed gasification system and separating and purifying a produced raw product gas, which solves at least one of the problems of the prior art, and reduces the amount of wastewater produced.
In order to achieve the first object of the present invention, the following technical solutions are adopted:
a fixed bed gasification system comprises a fixed bed gasification furnace, a scrubber and an oil scrubber which are sequentially connected through pipelines; wherein,
the fixed bed gasifier comprises a carbonaceous raw material inlet at the top, a gasifying agent inlet at the lower part, a crude product gas outlet at the upper part and an ash residue outlet at the bottom, wherein the gasifying agent inlet is communicated with a furnace core in the fixed bed gasifier and is used for introducing the carbonaceous raw material and the gasifying agent through the carbonaceous raw material inlet and the gasifying agent inlet respectively to carry out chemical reaction, ash residue is discharged from the ash residue outlet, and the crude product gas outlet comprises CH 4 、CO、CO 2 、H 2 And steam and carrying crude product gas of oil, phenol, ammonia and dust;
the scrubber is provided with a crude product gas inlet, a first wash oil inlet and an oil-gas mixture outlet, the crude product gas inlet is connected to the crude product gas outlet of the fixed bed gasifier and is used for inputting crude product gas from the fixed bed gasifier from the crude product gas inlet, introducing liquid wash oil from the first wash oil inlet to quench and wash the introduced crude product gas to remove part of dust and oil therein, and outputting an oil-gas mixture from the oil-gas mixture outlet;
The oil washing tower comprises an oil-gas mixture inlet positioned at the lower part, a second washing oil inlet positioned at the upper part and a top partA gas outlet and a dust-containing oil outlet at the bottom, wherein the oil-gas mixture inlet is connected to the oil-gas mixture outlet of the scrubber, and is used for introducing the oil-gas mixture from the scrubber from the oil-gas mixture inlet, introducing liquid washing oil from the second washing oil inlet to quench and wash the introduced oil-gas mixture, performing gas-liquid separation, outputting dust-containing oil containing dust, oil and phenol from the dust-containing oil outlet, and outputting dust-containing oil containing CH from the gas outlet 4 、CO、CO 2 And H 2 And the gas carrying ammonia and water vapor is used as the product gas.
Preferably, the fixed bed gasification system further comprises a first oil cooler, the oil scrubber further comprises an oil outlet positioned at the lower part, an inlet end of the first oil cooler is connected to the oil outlet of the oil scrubber, an outlet end of the first oil cooler is connected to a wash oil inlet of the oil scrubber and/or a first wash oil inlet of the scrubber, and the first oil cooler is used for cooling oil from the oil scrubber and then returning the cooled oil as liquid wash oil to the oil scrubber and/or the scrubber for recycling.
Preferably, the oil washing towers are sequentially connected in sequence; in the two adjacent oil washing towers, an oil-gas mixture inlet of a rear tower is connected to a gas outlet of a front tower, a dust-containing oil outlet of the rear tower is provided with a second oil cooler, and the outlet of the second oil cooler is respectively connected to at least one of a second washing oil inlet of the 1 st oil washing tower to the last 1 oil washing tower and a first washing oil inlet of the scrubber, and is used for returning materials output by the dust-containing oil outlet of the rear tower for recycling; and/or the number of the groups of groups,
The inside of the oil washing tower is sequentially divided into a plurality of layers of towers which are sequentially connected from top to bottom.
Preferably, the fixed bed gasification system further comprises a first separation unit; the first separation unit comprises a pressure reducing valve, a flash tank, an oil buffer tank, a centrifugal machine feeding pump, a centrifugal machine, an oil pressurizing pump, a third oil cooler and a flash gas scrubber; wherein,
the inlet of the pressure reducing valve is connected to a dust-containing oil outlet of the oil scrubber, and the outlet is respectively connected to inlets of the flash tank and the oil buffer tank and is used for reducing the pressure of dust-containing oil from the oil scrubber and then introducing the dust-containing oil into the flash tank and the oil buffer tank;
the flash tank comprises a gas phase outlet at the top and a liquid outlet at the bottom, and is used for carrying out flash evaporation separation on the introduced dust-containing oil, outputting flash evaporation gas containing non-condensable gas and oil vapor from an exhaust port of the flash tank, and discharging flash evaporation liquid containing dust and oil from the liquid outlet of the flash tank;
the flash gas scrubber comprises a flash gas inlet arranged at the lower part, a fourth wash oil inlet with a wash oil inlet arranged at the upper part, a non-condensable gas outlet arranged at the top part and a liquid phase outlet arranged at one side of the bottom part, wherein the flash gas inlet is connected to an exhaust port of the flash tank, the wash oil inlet is used for introducing liquid wash oil to cool and scrub the flash gas from the flash tank, the non-condensable gas is output from the non-condensable gas outlet, and a washing liquid phase containing oil is output from the liquid phase outlet;
The inlet of the oil buffer tank is respectively connected to the outlet of the pressure reducing valve, the liquid outlet of the flash tank and the liquid phase outlet of the flash gas scrubber, and is used for respectively receiving dust-containing oil from the pressure reducing valve, flash liquid from the flash tank and liquid phase from the flash gas scrubber, performing sedimentation separation, overflowing from the upper part to obtain clear oil, and settling from the bottom to obtain solid-containing oil;
the oil buffer tank, the oil pressurizing pump and the third oil cooler are sequentially connected, and an inlet of the oil pressurizing pump is connected to a clear oil outlet of the oil buffer tank and is used for pumping clear oil from the oil buffer tank to the third oil cooler for cooling under pressure and outputting first product oil;
the oil buffer tank, the centrifugal machine feed pump and the centrifugal machine are sequentially connected, an inlet of the centrifugal machine feed pump is connected to an oil-containing outlet of the oil buffer tank, and the oil-containing outlet is used for pumping the oil-containing oil from the oil buffer tank to the centrifugal machine for centrifugal dust removal, discharging second ash and outputting dust removal oil.
Preferably, the fixed bed gasification system further comprises a second separation unit; the second separation unit comprises an overhead oil cooler, an overhead reflux tank and a sewage pump which are connected in sequence; wherein,
The inlet of the tower top oil cooler is connected to the gas outlet of the oil scrubber, and is used for cooling the gas from the oil scrubber so as to condense oil vapor, water vapor and ammonia vapor in the gas to form condensate, so that a three-phase mixture material containing gas phase, oil phase and water phase is obtained; the tower top reflux tank is used for carrying out three-phase separation on the three-phase mixture from the tower top oil cooler, discharging sewage, outputting second product oil and outputting gas as product gas; the sewage pump is used for discharging sewage from the tower top reflux tank.
Preferably, the upper part of the oil washing tower is also provided with a third washing oil inlet; the second separation unit further comprises an overhead oil circulation pump, and its inlet end is connected to the second product oil outlet of the overhead reflux drum, and its outlet end is connected to the third wash oil inlet of the oil wash column for circulating the second product oil fraction from the overhead reflux drum to the oil wash column.
Preferably, the output pipeline of the sewage pump is also provided with a filter for filtering and outputting the sewage from the sewage pump;
preferably, the fixed bed gasification system further comprises a sewage heat exchanger and a stripping tower;
The sewage heat exchanger is arranged on a pipeline from the oil washing tower to the tower top oil cooler, a cold medium inlet of the sewage heat exchanger is connected to an outlet of a filter, a cold medium outlet of the sewage heat exchanger is connected to a cold medium inlet of the first oil cooler, and the sewage heat exchanger is used for carrying out heat exchange and temperature rise on materials from the filter by sequentially utilizing gas from the oil washing tower and oil from the oil outlet and outputting the materials from the cold medium outlet of the first oil cooler;
the gas stripping tower comprises a material inlet positioned at the upper part, an oxygen inlet and a water vapor inlet which are positioned at the middle part and are arranged from top to bottom, a gas stripping mixed gas outlet positioned at the top part and a sewage outlet positioned at the bottom part; the material inlet of the first oil cooler is connected with the cold medium outlet of the first oil cooler, and is used for introducing oxygen and water vapor to carry out stripping on the cold medium material from the first oil cooler, outputting stripping mixed gas from the stripping mixed gas outlet of the first oil cooler and discharging sewage from the sewage outlet of the first oil cooler;
the gas stripping mixed gas outlet of the gas stripping tower is connected to the gasifying agent inlet of the fixed bed gasifier and is used for returning the gas stripping mixed gas from the gas stripping tower to the fixed bed gasifier.
Preferably, a cooling water inlet is further arranged at the lower part of the fixed bed gasifier below the gasifying agent inlet and is used for supplementing cooling water to cool ash before discharging the ash;
Preferably, the fixed bed gasification system further comprises a third separation unit; the third separation unit comprises a lock hopper and a slag pool which are sequentially connected;
the top of the lock hopper is respectively provided with an ash inlet and a water outlet, the bottom of the lock hopper is provided with an ash outlet, and the ash inlet is connected to the ash outlet of the fixed bed gasifier and is used for collecting and decompressing ash water from the fixed bed gasifier, draining water from the water outlet to the slag pool and draining ash from the ash outlet to the slag pool; the ash inlet pipeline, the ash outlet pipeline and the water outlet pipeline of the lock hopper are respectively provided with a lock hopper inlet valve, a lock hopper outlet valve and a lock hopper drain valve;
the slag pool is also provided with an ash outlet and a water outlet, and the water outlet is connected to a cooling water inlet of the fixed bed gasifier and is used for separating slag from water of ash and water from the lock hopper, outputting the slag from the water outlet and returning the slag to the fixed bed gasifier; and a slag pool pump is arranged on a pipeline from the slag pool to the fixed bed gasifier.
Preferably, the fixed bed gasifier is provided with a water cooling wall; the lower part and the upper part of the shell of the fixed bed gasifier are respectively provided with a boiler water inlet and a boiler water outlet, and are used for leading in boiler water from the boiler water inlet and carrying out heat exchange and temperature rise on the water cooling wall to form a steam-water mixture and outputting the steam-water mixture from the boiler water outlet;
Preferably, the fixed bed gasification system further comprises a steam drum, wherein the steam drum is respectively provided with a steam inlet, a water outlet and a steam outlet, the steam inlet of the steam drum is connected to a boiler water outlet of the fixed bed gasification furnace, the water outlet of the steam drum is connected to a boiler water inlet of the fixed bed gasification furnace, the steam outlet of the steam drum is connected to the gasifying agent inlet, the steam drum is used for introducing a steam-water mixture from the fixed bed gasification furnace from the steam inlet of the steam drum to perform steam-water separation, water is output from the water outlet of the steam drum and circulated into a shell of the fixed bed gasification furnace, and water vapor is output from the steam outlet of the steam drum to a furnace core in the fixed bed gasification furnace to be used as the gasifying agent;
a boiler water circulation pump is arranged on a pipeline from a water outlet of the steam drum to a boiler water inlet of the fixed bed gasifier and is used for pumping the water circulation from the steam drum to a shell of the fixed bed gasifier.
To achieve the second object of the present invention, there is provided a fixed bed gasification method which is carried out using the aforementioned fixed bed gasification system.
Preferably, the fixed bed gasification process comprises:
(1) Introducing a carbonaceous raw material and a gasifying agent into the fixed bed gasifier respectively to carry out chemical reaction, discharging ash and slag, and self-discharging the ash and slag to contain CH 4 、CO、CO 2 、H 2 And steam and carrying crude product gas of oil, phenol, ammonia and dust;
(2) Introducing the obtained crude product gas into the scrubber, performing chilling washing by using the introduced liquid washing oil to remove part of dust and oil in the crude product gas, and outputting an oil-gas mixture;
(3) Introducing the obtained oil-gas mixture into the oil washing tower, performing chilling washing by using the introduced liquid washing oil, performing gas-liquid separation, and outputting dust-containing oil containing dust and phenol and CH-containing oil 4 、CO、CO 2 And H 2 And the gas carrying ammonia and water vapor is used as the product gas.
The invention has the beneficial effects that:
the fixed bed gasification system and the fixed bed gasification method of the invention have at least one of the following advantages:
(1) The product gas has good dust removal and purification effects. The oil washing dust removal technology is adopted, the capturing effect of oil on dust is good, and the efficient dust removal of product gas is facilitated; the efficient dust removal of the product gas is facilitated by a plurality of oil wash towers or a plurality of multi-layer washes in the oil wash towers (determined by the high service life of the catalyst and the inverse relation of the service life and the dust content in the obtained product gas when the obtained product gas is used in a subsequent conversion section).
(2) The energy utilization rate is high. By arranging the second oil cooler, sensible heat of the product gas is fully recovered, the circulating oil is cooled while the energy utilization rate is improved, and enough liquid wash oil is provided for oil washing.
(3) The sewage discharge amount is small. The product gas dust removal and purification adopts oil washing, avoids introducing water washing water, and the sewage after condensation and separation is only sourced from water vapor carried by the product gas, thereby greatly reducing the process wastewater.
(4) The sewage is easy to treat and can be directly sent to biochemical treatment. The phenol in the product gas is almost completely dissolved in the oil, the oil in the process sewage is also filtered by a filter, and the phenol and oil content in the sewage is low; the ammonia and acid gas in the sewage are further removed by adopting a gas stripping tower, and the treated sewage can be directly subjected to biochemical treatment.
(5) The oil is not easy to be blocked. According to the scheme, the temperature difference between the top and the bottom of the oil washing tower is controlled to be less than 50 ℃ (the circulating flow of liquid washing oil can be increased, or the load of the first oil cooler is reduced to improve the temperature of the liquid washing oil, so that the temperature difference between the top and the bottom of the oil washing tower is reduced, the fractionation of light oil and heavy oil can be reduced, dust-containing oil at the bottom of the oil washing tower contains partial light oil components, and asphalt blocking equipment and pipelines are not easy to generate. In addition, after ash is separated from dust-containing oil by decompression, the temperature of the clean oil which does not contain dust basically is reduced, and the clean oil is not easy to be blocked.
(6) The slag discharging system is simple. The slag discharging system adopts a hydraulic bucket locking slag discharging system, has a simple structure, and the bucket locking valve is lubricated by water flow, thereby being beneficial to prolonging the service life of the bucket locking.
(7) The safety performance is good. The gasification furnace adopts a water-cooling wall and pressure-bearing steel shell structure, the water-cooling wall is not pressure-bearing in heat insulation, the shell is not temperature-resistant in pressure bearing, and the safety performance is good.
(8) The gasification pressure is high. The operation pressure of the water-cooled wall is not limited by the gasification pressure, and the gasification pressure can be increased to 10MPaG. By increasing the gasification pressure, not only the subsequent system investment can be reduced, but also the single furnace production capacity can be improved.
(9) The gasification furnace can be added with more temperature measuring points, and the steam-oxygen ratio is convenient to control. The gasification furnace lining adopts a water-cooling wall system, a thermocouple can be arranged on the side wall of the water-cooling wall and inserted into the inner bed layer of the gasification furnace, and the temperature distribution of each layer (ash layer, combustion layer, gasification layer, carbonization layer and drying layer) in the gasification furnace can be accurately measured, so that the steam-oxygen ratio can be conveniently controlled, the steam-oxygen ratio can be controlled at a lower level, the steam consumption can be reduced, and the waste water production can be reduced.
Drawings
FIG. 1 is a schematic view of the structure of a fixed bed gasification system of the present invention in a first embodiment;
FIG. 2 is a schematic diagram of the structure of the fixed bed gasification system of the present invention in a second embodiment;
FIG. 3 is a schematic view of the structure of the fixed bed gasification system of the present invention in a third embodiment;
FIG. 4 is a schematic view of the structure of the fixed bed gasification system of the present invention in a fourth embodiment; .
FIG. 5 is a schematic view of the structure of the fixed bed gasification system of the present invention in a fifth embodiment;
FIG. 6 is a schematic view of the structure of the fixed bed gasification system of the present invention in a sixth embodiment;
FIG. 7 is a schematic view of the structure of a fixed bed gasification system of the present invention in a seventh embodiment;
FIG. 8 is a schematic diagram of the structure of a fixed bed gasification system of the present invention in an eighth embodiment;
fig. 9 is a schematic structural view of a fixed bed gasification system according to the present invention in a ninth embodiment.
Detailed Description
The technical scheme and effects of the present invention are further described below with reference to specific embodiments. The following embodiments/examples are only for illustrating the contents of the present invention, and the present invention is not limited to the following embodiments or examples. Simple modifications of the invention using the inventive concept are within the scope of the invention as claimed.
The invention provides a fixed bed gasification system, as shown in figure 1, which comprises a fixed bed gasification furnace 1, a scrubber 2 and an oil scrubber 3 which are sequentially connected through pipelines; wherein,
the fixed bed gasifier 1 comprises a carbonaceous raw material inlet 101 positioned at the top, a gasifying agent inlet 102 positioned at the lower part, a crude product gas outlet 103 positioned at the upper part and an ash outlet 104 positioned at the bottom, wherein the gasifying agent inlet 102 is communicated with a furnace core in the fixed bed gasifier 1 and is used for introducing the carbonaceous raw material and the gasifying agent through the carbonaceous raw material inlet 101 and the gasifying agent inlet 102 respectively to carry out chemical reaction, ash is discharged from the ash outlet 104, and CH is contained in the crude product gas outlet 103 4 、CO、CO 2 、H 2 And steam and carrying crude product gas of oil, phenol, ammonia and dust;
the scrubber 2 is provided with a crude product gas inlet 201, a first wash oil inlet 202 and an oil-gas mixture outlet 203, and the crude product gas inlet 201 is connected to the crude product gas outlet 103 of the fixed bed gasifier 1 and is used for inputting crude product gas from the fixed bed gasifier 1 from the crude product gas inlet 201, introducing liquid wash oil from the first wash oil inlet 202 to quench and wash the introduced crude product gas to remove part of dust and oil therein and outputting an oil-gas mixture from the oil-gas mixture outlet 203;
the oil scrubber 3 comprises an oil-gas mixture inlet 301 at the lower part, a second washing oil inlet 302 at the upper part, a gas outlet 303 at the top part and a dust-containing oil outlet 304 at the bottom part, wherein the oil-gas mixture inlet 301 is connected to the oil-gas mixture outlet 203 of the scrubber 2 and is used for introducing the oil-gas mixture from the scrubber 2 from the oil-gas mixture inlet 301, liquid washing oil is introduced from the second washing oil inlet 302 to quench and wash the introduced oil-gas mixture, gas-liquid separation is carried out, dust-containing oil containing dust, oil and phenol is output from the dust-containing oil outlet 304, and CH-containing oil is output from the gas outlet 303 4 、CO、CO 2 And H 2 And the gas carrying ammonia and water vapor is used as the product gas.
The fixed bed gasification system of the invention abandons the water washing method which is usually adopted, adopts the oil washing dust removal technology, has good dust capturing effect by utilizing oil, and is beneficial to realizing the high-efficiency dust removal of the product gas; the introduction of water washing water is avoided, the condensed and separated sewage is only derived from water vapor carried by product gas, the process wastewater quantity is greatly reduced, and the sewage discharge quantity is reduced; the phenol in the product gas can be removed by almost completely dissolving in the liquid wash oil.
Those skilled in the art understand that the carbonaceous feedstock includes coal, biomass, garbage, and the like; the gasifying agent comprises at least oxygen and may further comprise water vapor and/or carbon dioxide (i.e., the gasifying agent comprises any one of oxygen, oxygen and water vapor, oxygen and carbon dioxide, oxygen, water vapor and carbon dioxide). The chemical reaction of the carbonaceous raw material and the gasifying agent is combustion and gasification, and the generated products comprise CO and H 2 、CO 2 、H 2 O、CH 4 Tar, phenols, ammonia, ash, etc.
According to the fixed bed gasification system, the fractionation of light oil and heavy oil can be controlled and reduced by controlling the temperature difference between the top and the bottom of the oil washing tower (specifically, the temperature of the liquid washing oil can be increased by increasing the circulation flow of the liquid washing oil or reducing the load of the first oil cooler, so that the temperature difference between the top and the bottom of the oil washing tower is reduced), so that dust-containing oil at the bottom of the oil washing tower contains part of light oil components, and asphalt is not easy to generate to block equipment and pipelines.
In the present invention, the liquid wash oil may be any oil which can be used as a wash oil, including an oil separated from the crude product gas produced in the present invention, or an outsourced coal tar or the like.
Since the oil separated from the crude product gas produced by the present invention can also be used as the liquid wash oil of the scrubber 2 and/or the oil scrubber 3, in order to reduce the consumption and dust removal cost of the liquid wash oil and improve the energy utilization rate, in one embodiment, as shown in fig. 2, the fixed bed gasification system further comprises a first oil cooler 4, the oil scrubber 3 further comprises an oil outlet 305 positioned at the lower part, the inlet end of the first oil cooler 4 is connected to the oil outlet 305 of the oil scrubber 3, the outlet end is connected to the wash oil inlet of the oil scrubber 3 and/or the first wash oil inlet 202 of the scrubber 2, and the oil from the oil scrubber 3 is cooled and returned to the oil scrubber 3 and/or the scrubber 2 as the liquid wash oil for recycling.
In order to improve the dust removing effect, in one embodiment, as shown in fig. 3, the oil washing towers 3 are sequentially connected in sequence; and in the two adjacent oil wash towers 3, the oil-gas mixture inlet 301 of the rear tower is connected to the gas outlet 303 of the front tower, the dust-containing oil outlet 304 of the rear tower is provided with a second oil cooler 306, and the outlets of the second oil coolers 306 are respectively connected to at least one of the second wash oil inlets 302 of the 1 st to last 1 oil wash towers 3 and the first wash oil inlet 202 of the scrubber 2, and are used for returning the materials output by the dust-containing oil outlet 304 in the rear tower for recycling.
According to the invention, the second oil cooler is arranged, so that sensible heat of crude product gas can be fully recovered, the energy utilization rate is improved, meanwhile, the circulating oil is cooled, and enough liquid wash oil is provided for oil washing.
In order to improve the dust removing effect, in one embodiment, as shown in fig. 4, the inside of the oil washing tower 3 is divided into a plurality of layers of towers sequentially connected from top to bottom, so that the oil-gas mixture from the washing tower 2 is washed for multiple times, and the dust removing effect is improved.
In the operation process of the fixed bed gasification system, slag is required to be discharged in time, so that the gasification efficiency and the heat utilization rate are improved. In order to effectively remove slag in time, in one embodiment, as shown in fig. 5, the fixed bed gasification system further includes a first separation unit; the first separation unit comprises a pressure reducing valve 5, a flash tank 6, an oil buffer tank 7, a centrifugal feeding pump 8, a centrifugal machine 9, an oil pressurizing pump 10, a third oil cooler 11 and a flash gas scrubber 12; wherein,
the inlet of the pressure reducing valve 5 is connected to a dust-containing oil outlet 304 of the oil scrubber 3, and the outlets are respectively connected to inlets of the flash tank 6 and the oil buffer tank 7, and are used for reducing the pressure of dust-containing oil from the oil scrubber 3 and then introducing the dust-containing oil into the flash tank 6 and the oil buffer tank 7;
The flash tank 6 comprises a gas phase outlet at the top and a liquid outlet at the bottom, and is used for carrying out flash evaporation separation on the introduced dust-containing oil, outputting flash evaporation gas containing non-condensable gas and oil vapor from an exhaust port of the flash tank, and discharging flash evaporation liquid containing dust and oil from the liquid outlet of the flash tank;
the flash gas scrubber 12 comprises a flash gas inlet at the lower part, a fourth wash oil inlet with a wash oil inlet at the upper part, a non-condensable gas outlet at the top part and a liquid phase outlet at one side of the bottom part, wherein the flash gas inlet is connected to the exhaust port of the flash tank 6, the wash oil inlet is used for introducing liquid wash oil to cool and scrub the flash gas from the flash tank 6, the non-condensable gas is output from the non-condensable gas outlet, and the washing liquid phase containing oil is output from the liquid phase outlet;
the inlet of the oil buffer tank 7 is respectively connected to the outlet of the pressure reducing valve 5, the liquid outlet of the flash tank 6 and the liquid phase outlet of the flash gas scrubber 12, and is used for respectively receiving dust-containing oil from the pressure reducing valve 5, flash liquid from the flash tank 6 and liquid phase from the flash gas scrubber 12, performing sedimentation separation, overflowing from the upper part to obtain clear oil, and sedimentation from the bottom to obtain solid-containing oil;
The oil buffer tank 7, the oil pressurizing pump 10 and the third oil cooler 11 are sequentially connected, and an inlet of the oil pressurizing pump 10 is connected to a clear oil outlet of the oil buffer tank 7, and is used for pressurizing and pumping clear oil from the oil buffer tank 7 to the third oil cooler 11 for cooling and outputting first product oil;
the oil buffer tank 7, the centrifugal feeding pump 8 and the centrifugal 9 are sequentially connected, and an inlet of the centrifugal feeding pump 8 is connected to an oil-containing outlet of the oil buffer tank 7, and is used for pumping the oil-containing oil from the oil buffer tank 7 to the centrifugal 9 for centrifugal dust removal, discharging second ash and outputting dust-removing oil.
According to the invention, the dust-containing oil is decompressed firstly, ash residues are separated out to obtain the light oil which is basically free of dust, the temperature of the clear oil which is basically free of dust is reduced, and the first product oil is output, so that the clear oil is not easy to be blocked in a pipeline.
In one embodiment, as shown in fig. 5, the first separation unit further comprises a first return line 111, a first end of which is connected to the outlet of the third oil cooler 11, and a second end of which is connected to the fourth wash oil inlet of the flash gas scrubber 12 for returning the first product oil from the third oil cooler 11 to the flash gas scrubber 12, thereby improving the utilization of the oil produced during gasification.
In one embodiment, as shown in fig. 5, the first separation unit further comprises a second return line 91, a first end of which is connected to the de-dusting oil outlet of the centrifuge 9 and a second end of which is connected to the inlet of the oil buffer tank 7 for returning de-dusting oil from the centrifuge 9 to the oil buffer tank 7 for recycling.
In one embodiment, as shown in fig. 5, the first separation unit further comprises a third return line 81, the first end of which is connected to the outlet of the centrifuge feed pump 8 and the second end of which is connected to the inlet of the oil buffer tank 7 for returning the solid-containing oil from the centrifuge feed pump 8 to the oil buffer tank 7 for recycling.
In one embodiment, as shown in fig. 6, the fixed bed gasification system further comprises a second separation unit; the second separation unit comprises an overhead oil cooler 13, an overhead reflux tank 14 and a sewage pump 16 which are connected in sequence; wherein,
the inlet of the tower top oil cooler 13 is connected to the gas outlet 303 of the oil scrubber 3, and is used for cooling the gas from the oil scrubber 3 to condense oil vapor, water vapor and ammonia vapor into condensate, so as to obtain a three-phase mixed material comprising gas phase, oil phase and water phase; the tower top reflux tank 14 is used for carrying out three-phase separation on the three-phase mixture from the tower top oil cooler 13, discharging sewage and outputting second product oil and product gas; the sewage pump 16 is used to discharge sewage from the overhead reflux drum 14.
The invention is characterized in that an overhead oil cooler 13 is arranged at a gas outlet 303 of the oil scrubber 3, so that the gas from the oil scrubber 3 is cooled to condense oil vapor, water vapor and ammonia vapor into condensate for removal; by providing the tower top reflux tank 14 and the sewage pump 16, the materials output after condensate removal are subjected to three-phase separation, sewage is discharged, the second product oil is output, and the output gas is used as product gas.
In one embodiment, the upper part of the oil scrubber 3 is further provided with a third wash oil inlet; the second separation unit further comprises an overhead oil circulation pump 15, and an inlet end thereof is connected to a second product oil outlet of the overhead reflux drum 14, and an outlet end thereof is connected to a third wash oil inlet of the oil wash tower 3, for circulating a second product oil portion from the overhead reflux drum 14 to the oil wash tower 3, thereby providing liquid wash oil to the oil wash tower and improving the utilization rate of the oil produced during gasification.
In one embodiment, the third wash oil inlet is located above the second wash oil inlet 302 in the oil wash column 3 to facilitate receiving the second product oil from the overhead reflux drum 14.
In one embodiment, as shown in fig. 7, a filter 17 is further disposed on the output line of the sewage pump 16, for filtering the sewage from the sewage pump 16 and outputting the filtered sewage.
In the invention, the filter 17 is arranged to remove oil in the process sewage, and meanwhile, as phenol is mostly dissolved in the oil, the content of phenol and oil in the sewage discharged after being filtered by the filter 17 is low, thereby being beneficial to reducing the treatment difficulty and the treatment cost.
In one embodiment, the fixed bed gasification system further comprises a dirty water heat exchanger 18 and a stripper 19;
the sewage heat exchanger 18 is arranged on a pipeline from the oil scrubber 3 to the tower top oil cooler 13, and the cold medium inlet of the sewage heat exchanger is connected to the outlet of the filter 17, and the cold medium outlet of the sewage heat exchanger is connected to the cold medium inlet of the first oil cooler 4, so that the materials from the filter 17 are subjected to heat exchange and temperature rise by sequentially utilizing the gas from the oil scrubber 3 and the oil from the oil outlet 305 and are output from the cold medium outlet of the first oil cooler 4;
the stripping tower 19 comprises a material inlet at the upper part, an oxygen inlet and a water vapor inlet which are arranged from top to bottom at the middle part, a stripping mixed gas outlet at the top and a sewage outlet at the bottom; the material inlet of the device is connected to the cold medium outlet of the first oil cooler 4, and is used for introducing oxygen and water vapor to carry out stripping on the cold medium material from the first oil cooler 4, outputting stripping mixed gas from the stripping mixed gas outlet of the device and discharging sewage from the sewage outlet of the device;
The gas stripping mixture outlet of the gas stripping tower 19 is connected to the gasifying agent inlet 102 of the fixed bed gasifier 1 for returning the gas stripping mixture from the gas stripping tower 19 to the fixed bed gasifier 1.
According to the invention, ammonia and acid gas in the sewage can be further removed by arranging the gas stripping tower, so that the substances difficult to treat in the sewage are further reduced, and the sewage discharged after being treated by the gas stripping tower can be directly subjected to biochemical treatment, thereby being beneficial to reducing the treatment difficulty and the treatment cost.
In one embodiment, as shown in fig. 8, a cooling water inlet is further provided at a position lower than the gasifying agent inlet 102 at the lower part of the fixed bed gasifier 1, for supplementing cooling water to cool ash before discharging.
In one embodiment, as shown in fig. 8, the fixed bed gasification system further comprises a third separation unit; the third separation unit comprises a lock hopper 20 and a slag pool 21 which are sequentially connected;
the top of the lock hopper 20 is respectively provided with an ash inlet and a water outlet, the bottom of the lock hopper is provided with an ash outlet, and the ash inlet is connected to an ash outlet 104 of the fixed bed gasifier 1 and used for collecting and decompressing ash water from the fixed bed gasifier 1, draining the ash water from the water outlet to the ash pond 21 and draining the ash from the ash outlet to the ash pond 21; the ash inlet pipeline, the ash outlet pipeline and the water outlet pipeline of the lock hopper 20 are respectively provided with a lock hopper inlet valve, a lock hopper outlet valve and a lock hopper drain valve;
The slag bath 21 is also provided with an ash outlet and a water outlet, and the water outlet is connected to a cooling water inlet of the fixed bed gasifier 1 and is used for separating slag from water of ash and water from the lock hopper 20, and then the slag is output from the water outlet and returned to the fixed bed gasifier 1; a slag pool pump is arranged on a pipeline from the slag pool 21 to the fixed bed gasifier 1.
The hydraulic bucket locking slag discharging device adopts the hydraulic bucket locking slag discharging, has a simple structure, and the bucket locking valve is lubricated by water flow, thereby being beneficial to prolonging the service life of the bucket locking.
In one embodiment, as shown in fig. 9, the fixed bed gasifier 1 is provided with a water wall; the lower part and the upper part of the shell of the fixed bed gasification furnace 1 are respectively provided with a boiler water inlet and a boiler water outlet, and the boiler water inlet is used for leading in boiler water and the water cooling wall to exchange heat and raise temperature so as to form a steam-water mixture, and then the steam-water mixture is output from the boiler water outlet.
In the invention, the operation pressure of the water-cooled wall is not limited by the gasification pressure, and the gasification pressure can be increased to 10MPaG. By increasing the gasification pressure, not only the subsequent system investment can be reduced, but also the single furnace production capacity can be improved. Meanwhile, as the gasification furnace lining adopts the water-cooled wall, a thermocouple can be arranged on the side wall of the water-cooled wall and inserted into the inner bed layer of the gasification furnace, and the temperature distribution of each layer (ash layer, combustion layer, gasification layer, carbonization layer and drying layer) in the gasification furnace can be accurately measured, so that the steam-oxygen ratio can be conveniently controlled, the steam-oxygen ratio can be controlled at a lower level, and the steam consumption and the waste water production are reduced.
In one embodiment, the water wall is a pressure-bearing steel shell structure.
The fixed bed gasification system has good safety performance. The gasification furnace adopts a water-cooling wall and pressure-bearing steel shell structure, the water-cooling wall is not pressure-bearing in heat insulation, the shell is not temperature-resistant in pressure bearing, and the safety performance is good.
In one embodiment, as shown in fig. 9, the fixed bed gasification system further comprises a steam drum 22, wherein the steam drum 22 is respectively provided with a steam inlet, a water outlet and a steam outlet, the steam inlet is connected to a boiler water outlet of the fixed bed gasification furnace 1, the water outlet is connected to a boiler water inlet of the fixed bed gasification furnace 1, the steam outlet is connected to the gasifying agent inlet 102, the steam water mixture from the fixed bed gasification furnace 1 is introduced from the steam inlet to perform steam-water separation, water is output from the water outlet and circulated into a shell of the fixed bed gasification furnace 1, and water vapor is output from the steam outlet to a furnace core in the fixed bed gasification furnace 1 to be used as the gasifying agent;
a boiler water circulation pump 23 is provided on a line from the water outlet of the drum 22 to the boiler water inlet of the fixed bed gasifier 1 for pumping the water circulation from the drum 22 to the housing of the fixed bed gasifier 1.
The fixed bed gasification system can gasify the carbon-containing raw material, effectively separate and purify the produced crude product gas, and reduce the production amount of wastewater and the treatment difficulty.
The invention also provides a fixed bed gasification method which is carried out by using the fixed bed gasification system.
In one mode, as shown in fig. 1, the fixed bed gasification method includes:
(1) Introducing a carbonaceous raw material and a gasifying agent into the fixed bed gasifier 1 respectively to perform chemical reaction, discharging ash, and self-discharging the ash to contain CH 4 、CO、CO 2 、H 2 And steam and carrying crude product gas of oil, phenol, ammonia and dust;
(2) Introducing the obtained crude product gas into the scrubber 2, performing chilling washing by using the introduced liquid washing oil to remove part of dust and oil in the crude product gas, and outputting an oil-gas mixture;
(3) Introducing the obtained oil-gas mixture into the oil scrubber 3, performing chilling washing by using the introduced liquid washing oil, performing gas-liquid separation, and outputting dust-containing oil containing dust and phenol and CH-containing oil 4 、CO、CO 2 And H 2 And the gas carrying ammonia and water vapor is used as the product gas.
In one embodiment, in step (1), the reaction conditions include: the reaction pressure is 0.1 to 10MPaG, such as 2MPaG, 4MPaG, 6.5MPaG and 8MPaG; the reaction temperature is 800 to 1100 ℃, such as 900 ℃ and 1000 ℃.
In the present invention, the reaction temperature in step (1) is lower than the ash melting point of the carbonaceous feedstock.
In one embodiment, the temperature of the raw product gas obtained in step (1) is 200 to 600 ℃, such as 300 ℃, 400 ℃ and 500 ℃.
In one embodiment, in step (2), the temperature of the liquid wash oil introduced is from 100 to 500 ℃, such as 200 ℃, 300 ℃ and 400 ℃.
In one embodiment, in step (3), the temperature of the liquid wash oil introduced is from 100 to 500 ℃, such as 200 ℃, 300 ℃ and 400 ℃.
In one embodiment, as shown in fig. 2, in step (3), the oil scrubber 3 further outputs oil containing dust from an oil outlet 305 thereof, and the fixed bed gasification method further includes cooling the oil outputted from the oil outlet 305 thereof and returning the cooled oil as liquid wash oil to the oil scrubber 3 and/or the scrubber 2 for recycling.
In one embodiment, as shown in fig. 3, in the step (3), the obtained oil-gas mixture is introduced into at least 2 oil washing towers 3 connected in series, and chilled washing is performed at least 2 times by using the introduced liquid washing oil, dust-containing oil containing dust and phenol is discharged from the bottom of the 1 st oil washing tower 3, and the top output of the last 1 oil washing tower 3 contains CH 4 CO and H 2 And the gas carrying ammonia and water vapor is used as the product gas. Preferably, the bottom materials of the 2 nd oil scrubber 3 and the following oil scrubber 3 are respectively returned to any one or more of the 1 st to last 1 st oil scrubber 3 and the scrubber 2 to be recycled as liquid wash oil thereof.
In one embodiment, as shown in FIG. 4, in the step (3), the obtained oil-gas mixture is introduced into the oil scrubber 3 provided in a multi-layer column to be washed a plurality of times, dust-containing oil containing dust and phenol is discharged from the bottom, and CH is contained in the oil-containing oil is discharged from the top of the column 4 、CO、CO 2 And H 2 And the gas carrying ammonia and water vapor is used as the product gas.
In one embodiment, in step (3), the temperature at the top and/or the temperature at the bottom of the oil scrubber 3 is 100 to 500 ℃ (e.g., 200 ℃, 300 ℃ and 400 ℃) and the temperature difference between the top and the bottom is less than 50 ℃ (e.g., 40 ℃, 30 ℃, 20 ℃ and 10 ℃).
In one embodiment, as shown in fig. 5, the fixed bed gasification method further includes a step (4) of passing the dust-containing oil discharged from the step (3) to a first separation unit for separation treatment. In one embodiment, the step (4) is to discharge the dust-containing oil discharged from the step (3) into a first separation unit, decompress (preferably decompress to normal pressure), flash-separate a part of the dust-containing oil to output flash vapor containing noncondensable gas and oil vapor and flash liquid containing dust and oil, wash the output flash gas, discharge the noncondensable gas to a flare line, and output a washing liquid phase; and the other part of the clear oil overflowed from the upper part is cooled and then partially used as first product oil to be output, and the other part of the clear oil is used as liquid wash oil of flash steam, and part of the solid-containing oil obtained by settling from the bottom is directly returned to the oil buffer tank 7 so as to avoid blockage of centrifugal equipment during offline maintenance, and the other part of the solid-containing oil is returned to the oil buffer tank 7 after centrifugal separation and dust removal and is discharged to ash slag.
In one embodiment, as shown in fig. 6, the fixed bed gasification method further includes a step (5) of passing the product gas outputted from the step (3) to a second separation unit for separation treatment. In one embodiment, the step (5) is to cool the product gas output in the step (3) in a second separation unit (preferably to 0-60 ℃) and then condense the oil vapor, the water vapor and the ammonia vapor into condensate to obtain a three-phase mixture material comprising a gas phase, an oil phase and a water phase; then the three-phase mixture obtained after cooling is sent into the tower top reflux tank 14 for three-phase separation, the sewage obtained by separation is discharged through the sewage pump 16, part of the oil obtained by separation is used as second product oil to be output, and the other part of the oil is returned into the oil scrubber 3 through the tower top circulating pump 15, and the separation output contains CO and H 2 、CO 2 、CH 4 Is a product gas of (a) a product gas of (b).
In one embodiment, as shown in fig. 7, step (5) further includes filtering and heating the sewage discharged from the sewage pump 16, and then delivering the sewage to the stripping tower 19 for stripping, discharging the sewage, and outputting a stripping gas mixture.
In the invention, oxygen and water vapor are also sent to the stripping tower, and the acid gas and ammonia in the sewage after filtration and temperature rising are stripped out through the oxygen and the water vapor in the stripping tower, and part of the sewage is vaporized into water vapor.
In a preferred embodiment, as shown in fig. 7, in step (5), the temperature of the sewage discharged from the sewage pump 16 is raised after filtering, by sending the sewage to the sewage heat exchanger 18 to exchange heat with the product gas outputted from step (3), and then sending the sewage to the first oil cooler 4 to exchange heat with the oil from the oil outlet 305 of the oil scrubber 3.
In a preferred embodiment, as shown in fig. 7, the product gas separated in step (5) is returned to the fixed bed gasifier 1 through the gasifying agent inlet 102 of the fixed bed gasifier 1 to be used as a gasifying agent.
In one embodiment, as shown in fig. 8, in the step (1), the fixed bed gasifier 1 is supplemented with cooling water through its cooling water inlet to cool ash before it is discharged, and then discharged with water, i.e., ash water.
In a preferred embodiment, as shown in fig. 8, the fixed bed gasification method further includes a step (6) of passing the ash water discharged from the step (1) to a third separation unit for separation treatment. In one embodiment, the step (6) is to introduce the ash water discharged from the step (1) into a third separation unit, collect the ash and release the pressure (release the pressure to normal pressure) through the lock hopper 20, and drain the ash and the ash from the water outlet and the ash outlet respectively into the slag pool 21 to separate the slag and the water, discharge the ash and output the water.
In a preferred embodiment, as shown in fig. 8, the water outputted in the step (6) is returned to the fixed bed gasifier 1 through the cooling water inlet of the fixed bed gasifier 1 to be supplemented, and the water supplementing flow is preferably 10-50 m 3 /h, e.g. 20m 3 /h、30m 3 /h and 40m 3 /h。
In one embodiment, as shown in fig. 9, the fixed bed gasification method further includes a step (7) of introducing boiler water into the shell of the fixed bed gasification furnace 1 from the boiler water inlet, performing heat exchange with the water-cooled wall thereof to raise the temperature, forming a steam-water mixture, and outputting the steam-water mixture from the boiler water outlet thereof, thereby cooling the water-cooled wall.
In one embodiment, as shown in fig. 9, the fixed bed gasification method further includes a step (8), where in the step (8) is to introduce the steam-water mixture outputted in the step (7) into the steam drum 22 to perform steam-water separation, output water from the water outlet thereof and circulate the water into the shell of the fixed bed gasification furnace 1, and output water vapor from the steam outlet thereof to the furnace core in the fixed bed gasification furnace 1 to be used as a gasification agent.
It is understood by those skilled in the art that the fixed bed gasification system and the fixed bed gasification method of the present invention are all common devices in the art, and the pipeline may be provided with a corresponding lift pump or booster pump to facilitate the transportation of materials in the pipeline, a valve may be provided to control the transportation of materials in the pipeline, and a corresponding buffer tank may be provided for the corresponding materials to facilitate the buffering and storage of the corresponding materials, which is not described in detail.
The fixed bed gasification system and the fixed bed gasification method of the invention have at least one of the following effects: the product gas has good dust removal and purification effects; the energy utilization rate is high; the sewage discharge amount is small; the sewage can be directly sent to biochemical treatment, and is easy to treat; the oil is not easy to be blocked; the slag is simply discharged; the safety performance is good; the gasification pressure is high, the subsequent system investment can be reduced, and the single-furnace production capacity can be improved; the gasification furnace can be added with more temperature measuring points, the steam-oxygen ratio is convenient to control, and the steam-oxygen ratio can be controlled at a lower level, so that the steam consumption is reduced, and the wastewater production is reduced.
The raw materials used in the following examples and comparative examples of the present invention are as follows:
the carbonaceous raw material is bituminous coal, and specific information of the bituminous coal is shown in table 1;
the liquid wash oil is a second product oil produced by self, and specific information is shown in table 2;
TABLE 1 analysis of bituminous coal
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TABLE 2 physical Properties of liquid wash oil
| Project | Unit (B) | Properties of (C) |
| Density (20 ℃ C.) | g/cm 3 | 0.98～1.06 |
| Viscosity (60 ℃ C.) | mm 2 /s | 50 |
The method for measuring/calculating the relevant parameters is as follows:
the components of the sewage are determined by adopting a Nahner reagent spectrophotometry for determining ammonia nitrogen in HJ535-2009 water quality; measuring the phenol content in the sewage by adopting a direct bromination method; determining the oil content in the sewage by adopting an infrared photometry method for determining HJ 637-2012 water quality petroleum and animal and vegetable oil; the COD value in the sewage is measured by adopting a quick digestion spectrophotometry method for measuring the chemical oxygen demand of the water quality of HJ/T399-2007.
Example 1 (S1)
The carbonaceous feedstock was subjected to fixed bed gasification using a fixed bed gasification system as shown in FIG. 1, according to a single furnace carbonaceous feedstock throughput of 650t/d, comprising the steps of:
(1) Introducing a carbonaceous raw material and a gasifying agent into the fixed bed gasifier 1 respectively to perform chemical reaction, discharging ash, and self-discharging the ash to contain CH 4 、CO、CO 2 、H 2 And steam and carrying crude product gas of oil, phenol, ammonia and dust; wherein the carbonaceous raw material is bituminous coal, and the inlet flow is 27.2t/h; the gasifying agent is oxygen and water vapor, and the flow rates are 6796Nm respectively 3 /h and 23.7t/h; the reaction conditions include: the operating temperature is 1100 ℃, and the operating pressure is 3.5MPaG;
(2) Introducing the obtained crude product gas into the scrubber 2, performing chilling washing by using the introduced liquid washing oil to remove part of dust and oil in the crude product gas, and outputting an oil-gas mixture; wherein the introduced liquid wash oil is self-produced second product oil with temperature of 260 ℃ and flow rate of 20m 3 /h；
(3) Introducing the obtained oil-gas mixture into the oil scrubber 3, performing chilling washing by using the introduced liquid washing oil, performing gas-liquid separation, and outputting dust-containing oil containing dust and phenol and CH-containing oil 4 、CO、CO 2 And H 2 And the gas carrying ammonia and water vapor is used as the product gas; wherein the introduced liquid wash oil is self-produced second product oil with temperature of 260 ℃ and flow rate of 150m 3 /h；。
Example 2 (S2)
The carbonaceous feedstock was subjected to fixed bed gasification using a fixed bed gasification system as shown in fig. 2, wherein the fixed bed gasification method only differs from example 1 in that:
in the step (3), the oil washer 3 outputs oil from the oil outlet 305, and the oil outputted from the oil outlet 305 is cooled to 260 ℃ by the first oil cooler 4 and then returned to the oil washer 3 and the washer 2 as liquid wash oil for recycling.
Example 3 (S3)
The carbonaceous feedstock was subjected to fixed bed gasification using a fixed bed gasification system as shown in fig. 3, wherein the fixed bed gasification method only differs from example 1 in that:
in the step (3), the obtained oil-gas mixture is introduced into 2 oil washing towers 3 connected in series to carry out 2 times of chilling washing by using the introduced liquid washing oil, dust-containing oil containing dust and phenol is discharged from the bottom of the 1 st oil washing tower 3, and CH is contained in the top output of the 2 nd oil washing tower 3 4 、CO、CO 2 And H 2 And the gas carrying ammonia and water vapor is used as the product gas; and the bottom materials of the 2 nd oil washing tower 3 are respectively returned to the 1 st oil washing tower 3, the 2 nd oil washing tower 3 and the scrubber 2 to be recycled as liquid washing oil thereof.
Example 4 (S4)
The carbonaceous feedstock was subjected to fixed bed gasification using a fixed bed gasification system as shown in fig. 4, wherein the fixed bed gasification method only differs from example 1 in that:
in the step (3), the obtained oil-gas mixture is introduced into the oil washing tower 3 arranged in a multi-layer tower for washing for a plurality of times, dust-containing oil containing dust and phenol is discharged from the bottom, and CH is discharged from the top of the tower 4 、CO、CO 2 And H 2 And the gas carrying ammonia and water vapor is used as the product gas.
Example 5 (S5)
The carbonaceous feedstock was subjected to fixed bed gasification using a fixed bed gasification system as shown in fig. 5, wherein the fixed bed gasification method only differs from example 1 in that:
the method also comprises a step (4) of introducing the dust-containing oil discharged from the step (3) into a first separation unit for separation treatment, wherein the method comprises the following steps: introducing the dust-containing oil discharged in the step (3) into a first separation unit, decompressing to normal pressure through a decompression valve 5, then sending a part of the oil into a flash tank 6 for flash separation, outputting flash steam containing noncondensable gas and oil steam and flash liquid containing dust and oil, sending the output flash steam into a flash gas scrubber 12 for washing, then discharging the noncondensable gas to a torch pipeline, and outputting a washing liquid phase; the other part of the clear oil obtained by overflowing from the upper part is lifted and pumped into the third oil cooler 11 through an oil pressurizing pump 10 to be cooled, the other part of the clear oil is returned into a flash gas scrubber 12 to be used as liquid wash oil of flash steam, solid oil obtained by settling from the bottom is lifted and pumped through a centrifugal feeding pump 8, one part of the solid oil is directly returned into the oil buffer tank 7 to avoid blockage of centrifugal equipment during offline maintenance, and the other part of the solid oil is sent into the centrifugal machine 9 to be returned into the oil buffer tank 7 after centrifugal separation and dust removal to discharge ash slag.
Example 6 (S6)
The carbonaceous feedstock was subjected to fixed bed gasification using a fixed bed gasification system as shown in fig. 6, wherein the fixed bed gasification method only differs from example 5 in that:
the method also comprises a step (5) of introducing the product gas output from the step (3) into a second separation unit for separation treatment, wherein the method comprises the following steps: the product gas output in the step (3) is led into a second separation unit, cooled to 40 ℃ by an overhead oil cooler 13, and then oil vapor, water vapor and ammonia vapor in the product gas are condensed into condensate, so as to obtain a three-phase mixture material containing gas phase, oil phase and water phase; then the three-phase mixture obtained after cooling is sent into the tower top reflux tank 14 for three-phase separation, the sewage obtained by separation is discharged through the sewage pump 16, part of the oil obtained by separation is used as second product oil to be output, and the other part of the oil is returned into the oil scrubber 3 through the tower top circulating pump 15, and the separation output contains CO and H 2 、CO 2 、CH 4 Is a product gas of (a) a product gas of (b).
Example 7 (S7)
The carbonaceous feedstock was subjected to fixed bed gasification using a fixed bed gasification system as shown in fig. 7, wherein the fixed bed gasification method only differs from example 6 in that:
in the step (5), before the product gas output in the step (3) is led into the tower top oil cooler 13, the product gas is firstly led into the sewage heat exchanger 18 for cooling; step (5) further comprises filtering and deoiling the sewage discharged by the sewage pump 16 in a filter 17, sequentially delivering to a sewage heat exchanger 18 and a first oil cooler 4 to exchange heat with the product gas output by step (3), heating, delivering to a stripping tower 19 for stripping (simultaneously introducing oxygen and water vapor into the stripping tower 19), discharging sewage, outputting a stripping mixed gas, and returning to the fixed bed gasifier 1 from a gasifying agent inlet 102 of the fixed bed gasifier 1 to be used as a gasifying agent.
Example 8 (S8)
The carbonaceous feedstock was subjected to fixed bed gasification using a fixed bed gasification system as shown in fig. 8, wherein the fixed bed gasification method only differs from example 7 in that:
the method also comprises a step (6) of introducing the ash water discharged from the step (1) into a third separation unit for separation treatment, wherein the steps are as follows: introducing the ash water discharged in the step (1) into a third separation unit, carrying out slag collection and pressure relief (pressure relief to normal pressure) through the lock hopper 20, respectively discharging water and ash slag into the slag pool 21 from a water outlet and an ash slag outlet of the third separation unit, discharging ash slag, lifting output water through a slag pool pump, and returning the output water to the fixed bed gasification furnace 1 from a cooling water inlet of the fixed bed gasification furnace 1 for water supplementing.
Example 9 (S9)
The carbonaceous feedstock was subjected to fixed bed gasification using a fixed bed gasification system as shown in fig. 9, wherein the fixed bed gasification method only differs from example 7 in that:
the method also comprises the step (7) of leading the boiler water into the shell of the fixed bed gasification furnace 1 from the boiler water inlet, carrying out heat exchange and heating with the water-cooling wall to form a steam-water mixture, and outputting the steam-water mixture from the boiler water outlet so as to cool the water-cooling wall;
And step (8) of introducing the steam-water mixture output in the step (7) into the steam drum 22 for steam-water separation, outputting water from a water outlet thereof and circulating the water from a boiler water inlet into the shell of the fixed bed gasifier 1, outputting water vapor from a steam outlet thereof and circulating the water vapor from a gasifying agent inlet 102 to a furnace core in the fixed bed gasifier 1 to be used as a gasifying agent.
Results:
examples 1-5 (S1-5) were analyzed and found to have no effluent discharge, i.e., a effluent displacement of 0, but the resulting product gas contained oil and ammonia, which required further treatment.
The product gas obtained in examples 6 to 9 (S6 to 9) and the product gas obtained by the conventional method using water chilling washing were used in the subsequent shift section, and catalyst life was measured, and the measurement results are shown in Table 3 (the dust content in the product gas affects the life of the catalyst in the subsequent shift section, and the two are inversely proportional).
Service life of catalyst in the case where the product gas obtained in Table 3 was used in the subsequent shift section
According to Table 3, in the embodiment of the invention, the service life of the catalyst is as long as 2 years when the obtained product gas is used in the subsequent conversion section, and accordingly, the dust content of the catalyst is relatively small, compared with the service life of the catalyst is only 1.5 years when the product gas obtained by the traditional method of water chilling washing is used in the subsequent conversion section, and accordingly, the dust content of the catalyst is relatively large, and the quality of the product gas obtained by the embodiment of the invention is effectively improved.
The wastewater discharged in examples 6 to 9 (S6 to 9) was analyzed, and the analysis results are shown in Table 4.
Table 4 shows the results of analysis of the sewage discharged from the reactor
Note that: the sewage discharge amount in Table 4 was calculated according to the treatment amount of the carbonaceous material in the single furnace of 650 t/d.
As can be seen from Table 2, in the embodiment 6 of the present invention, the sewage discharge amount is 14.6t/h, and the oil and ammonia in the product gas are condensed into condensate which is discharged with the sewage, so that the oil and ammonia content in the discharged sewage is high, and the COD value is large; compared with the traditional method adopting water chilling washing, the sewage discharge amount of the sewage discharged by the traditional method is up to 26t/h, so that the sewage discharge amount is greatly reduced;
in the embodiments 7 to 9 of the invention, the discharge capacity of the discharged sewage is as low as 2t/h, and the discharged sewage of the embodiment 6 is further treated, so that the ammonia content in the discharged sewage is as low as 200mg/L, the phenolic content is as low as 600mg/L, the oil content is as low as 10mg/L, COD and as low as 800mg/L, the discharged sewage can be directly sent to biochemical treatment, and the treatment difficulty is low; compared with the traditional method of water chilling washing, the discharge amount of the sewage discharged by the traditional method is up to 26t/h, the ammonia content in the sewage discharged by the prior art is up to 4000-9000 mg/L, the phenolic content is up to 6000-10000 mg/L, the oil content is up to 300-600 mg/L, COD and is up to 3000-5000 mg/L, the treatment difficulty is high, the discharge amount of the sewage discharged by the invention of the embodiment 7-9 is greatly reduced, the contents of ammonia, phenols, oils and COD in the discharged sewage are greatly reduced, and the treatment difficulty is also greatly reduced.
Compared with the traditional method adopting water chilling washing, the fixed bed gasification system and the fixed bed gasification method of the invention in the embodiments 1-9 are simple and easy to operate, and have at least one of the following effects: the obtained product gas has low dust content and good dust removal and purification effects; the sewage discharge amount is small; the content of the components which are difficult to treat in the discharged sewage is low, and the discharged sewage can be directly sent to biochemical treatment and is easy to treat.
Claims (10)
1. A fixed bed gasification system, which is characterized by comprising a fixed bed gasification furnace (1), a scrubber (2) and an oil scrubber (3) which are sequentially connected through pipelines; wherein,
the fixed bed gasifier (1) comprises a carbonaceous raw material inlet (101) at the top, a gasifying agent inlet (102) at the lower part, a crude product gas outlet (103) at the upper part and an ash residue outlet (104) at the bottom, wherein the gasifying agent inlet (102) is communicated with a furnace core in the fixed bed gasifier (1) and is used for introducing carbonaceous raw materials and gasifying agents through the carbonaceous raw material inlet (101) and the gasifying agent inlet (102) respectively to carry out chemical reaction, ash residues are discharged from the ash residue outlet (104), and the crude product gas outlet (103) outputs a catalyst containing CH 4 、CO、CO 2 、H 2 And steam and carrying crude product gas of oil, phenol, ammonia and dust;
The scrubber (2) is provided with a crude product gas inlet (201), a first wash oil inlet (202) and an oil-gas mixture outlet (203), and the crude product gas inlet (201) is connected to the crude product gas outlet (103) of the fixed bed gasifier (1) and is used for inputting the crude product gas from the fixed bed gasifier (1) from the crude product gas inlet (201), introducing liquid wash oil from the first wash oil inlet (202) to quench and wash the introduced crude product gas to remove part of dust and oil, and outputting the oil-gas mixture from the oil-gas mixture outlet (203);
the oil scrubber (3) comprises an oil gas mixture inlet (301) at the lower part, a second washing oil inlet (302) at the upper part, a gas outlet (303) at the top part and a dust-containing oil outlet (304) at the bottom part, wherein the oil gas mixture inlet (301) is connected to the oil gas mixture outlet (203) of the scrubber (2) and is used for introducing the oil gas mixture from the scrubber (2) from the oil gas mixture inlet (301), liquid washing oil is introduced from the second washing oil inlet (302) to perform gas-liquid separation after chilling washing on the introduced oil gas mixture, dust-containing oil containing dust, oil and phenol is output from the dust-containing oil outlet (304), and CH is contained in the gas mixture output from the gas outlet (303) 4 、CO、CO 2 And H 2 And the gas carrying ammonia and water vapor is used as the product gas.
2. The fixed bed gasification system according to claim 1, further comprising a first oil cooler (4), the oil scrubber (3) further comprising an oil outlet (305) located at the lower part, the inlet end of the first oil cooler (4) being connected to the oil outlet (305) of the oil scrubber (3), the outlet end being connected to the wash oil inlet of the oil scrubber (3) and/or the first wash oil inlet (202) of the scrubber (2) for cooling the oil from the oil scrubber (3) and returning it to the oil scrubber (3) and/or the scrubber (2) for recycling as liquid wash oil.
3. A fixed bed gasification system according to claim 1 or 2,
the plurality of the oil washing towers (3) are sequentially connected in sequence; in the two adjacent oil washing towers (3), an oil-gas mixture inlet (301) of a rear tower is connected to a gas outlet (303) of a front tower, a dust-containing oil outlet (304) of the rear tower is provided with a second oil cooler (306), and the outlets of the second oil coolers (306) are respectively connected to at least one of a second washing oil inlet (302) of the 1 st oil washing tower (3) to the last 1 first washing oil inlet (202) of the washer (2) and are used for returning materials output by the dust-containing oil outlet (304) of the rear tower for recycling; and/or the number of the groups of groups,
The inside of the oil washing tower (3) is sequentially divided into a plurality of layers of towers which are sequentially connected from top to bottom.
4. A fixed bed gasification system according to any one of claims 1 to 3 wherein,
the fixed bed gasification system further comprises a first separation unit; the first separation unit comprises a pressure reducing valve (5), a flash tank (6), an oil buffer tank (7), a centrifugal feeding pump (8), a centrifugal machine (9), an oil pressurizing pump (10), a third oil cooler (11) and a flash gas scrubber (12); wherein,
the inlet of the pressure reducing valve (5) is connected to a dust-containing oil outlet (304) of the oil scrubber (3), and the outlets are respectively connected to inlets of the flash tank (6) and the oil buffer tank (7) and are used for reducing the pressure of dust-containing oil from the oil scrubber (3) and then introducing the dust-containing oil into the flash tank (6) and the oil buffer tank (7);
the flash tank (6) comprises a gas phase outlet at the top and a liquid outlet at the bottom, and is used for carrying out flash separation on the introduced dust-containing oil, outputting flash gas containing non-condensable gas and oil steam from an exhaust port of the flash tank, and discharging flash liquid containing dust and oil from the liquid outlet of the flash tank;
the flash gas scrubber (12) comprises a flash gas inlet arranged at the lower part, a fourth wash oil inlet arranged at the upper part and provided with a wash oil inlet, a non-condensable gas outlet arranged at the top part and a liquid phase outlet arranged at one side of the bottom part, the flash gas inlet is connected to the exhaust port of the flash tank (6), the wash oil inlet is used for introducing liquid wash oil to cool and scrub the flash gas from the flash tank (6), the non-condensable gas outlet outputs non-condensable gas, and the liquid phase outlet outputs a washing liquid phase containing oil;
The inlet of the oil buffer tank (7) is respectively connected to the outlet of the pressure reducing valve (5), the liquid outlet of the flash tank (6) and the liquid phase outlet of the flash gas scrubber (12) and is used for respectively receiving dust-containing oil from the pressure reducing valve (5), flash liquid from the flash tank (6) and liquid phase from the flash gas scrubber (12) and performing sedimentation separation, overflowing from the upper part to obtain clear oil and sedimentation from the bottom to obtain solid-containing oil;
the oil buffer tank (7), the oil pressurizing pump (10) and the third oil cooler (11) are sequentially connected, and an inlet of the oil pressurizing pump (10) is connected to a clear oil outlet of the oil buffer tank (7) and is used for pressurizing and pumping clear oil from the oil buffer tank (7) to the third oil cooler (11) for cooling and outputting first product oil;
the oil buffer tank (7), the centrifugal feeding pump (8) and the centrifugal machine (9) are sequentially connected, and an inlet of the centrifugal feeding pump (8) is connected to an oil-containing outlet of the oil buffer tank (7) and is used for pumping the oil-containing oil from the oil buffer tank (7) to the centrifugal machine (9) for centrifugal dust removal, discharging second ash slag and outputting dust removal oil.
5. A fixed bed gasification system according to any one of claims 1 to 4 wherein,
The fixed bed gasification system further comprises a second separation unit; the second separation unit comprises an overhead oil cooler (13), an overhead reflux tank (14) and a sewage pump (16) which are connected in sequence; wherein,
the inlet of the tower top oil cooler (13) is connected to a gas outlet (303) of the oil scrubber (3) and is used for cooling gas from the oil scrubber (3) to condense oil vapor, water vapor and ammonia vapor in the gas to form condensate, so as to obtain a three-phase mixture material comprising gas phase, oil phase and water phase; the tower top reflux tank (14) is used for carrying out three-phase separation on the three-phase mixture from the tower top oil cooler (13), discharging sewage, outputting second product oil and outputting gas as product gas; the sewage pump (16) is used for discharging sewage from the tower top reflux tank (14);
preferably, the upper part of the oil washing tower (3) is also provided with a third washing oil inlet; the second separation unit further comprises an overhead oil circulation pump (15) with its inlet end connected to the second product oil outlet of the overhead reflux drum (14) and its outlet end connected to the third wash oil inlet of the oil wash column (3) for circulating the second product oil fraction from the overhead reflux drum (14) to the oil wash column (3);
Preferably, the third wash oil inlet is higher than the second wash oil inlet (302).
6. A fixed bed gasification system as set forth in claim 5 wherein,
a filter (17) is further arranged on an output pipeline of the sewage pump (16) and is used for filtering and outputting sewage from the sewage pump (16);
preferably, the fixed bed gasification system further comprises a sewage heat exchanger (18) and a stripper (19);
the sewage heat exchanger (18) is arranged on a pipeline from the oil washing tower (3) to the overhead oil cooler (13), the cold medium inlet of the sewage heat exchanger is connected to the outlet of the filter (17), the cold medium outlet of the sewage heat exchanger is connected to the cold medium inlet of the first oil cooler (4), and the sewage heat exchanger is used for carrying out heat exchange and temperature rise on materials from the filter (17) and outputting the materials from the cold medium outlet of the first oil cooler (4) by sequentially utilizing gas from the oil washing tower (3) and oil from the oil outlet (305);
the stripping tower (19) comprises a material inlet at the upper part, an oxygen inlet and a water vapor inlet which are arranged in the middle part from top to bottom, a stripping mixed gas outlet at the top and a sewage outlet at the bottom; the material inlet of the device is connected to a cold medium outlet of the first oil cooler (4) and is used for introducing oxygen and water vapor to carry out gas stripping on the cold medium material from the first oil cooler (4), and the gas stripping mixed gas is output from a gas stripping mixed gas outlet and the sewage is discharged from a sewage outlet;
The stripping mixed gas outlet of the stripping tower (19) is connected to the gasifying agent inlet (102) of the fixed bed gasifier (1) and is used for returning the stripping mixed gas from the stripping tower (19) to the fixed bed gasifier (1).
7. A fixed bed gasification system according to any one of claims 1 to 6,
the lower part of the fixed bed gasifier (1) is lower than the gasifying agent inlet (102) and is also provided with a cooling water inlet for supplementing cooling water to cool the ash before discharging;
preferably, the fixed bed gasification system further comprises a third separation unit; the third separation unit comprises a lock hopper (20) and a slag pool (21) which are sequentially connected;
the top of the lock hopper (20) is respectively provided with an ash inlet and a water outlet, the bottom of the lock hopper is provided with an ash outlet, and the ash inlet is connected to an ash outlet (104) of the fixed bed gasifier (1) and is used for collecting and decompressing ash water from the fixed bed gasifier (1), draining water to the slag pool (21) from the water outlet and draining ash to the slag pool (21) from the ash outlet; the ash inlet pipeline, the ash outlet pipeline and the water outlet pipeline of the lock hopper (20) are respectively provided with a lock hopper inlet valve, a lock hopper outlet valve and a lock hopper drain valve;
The slag pool (21) is also provided with an ash outlet and a water outlet, and the water outlet is connected to a cooling water inlet of the fixed bed gasifier (1) and is used for separating ash from water from the lock hopper (20) and then outputting the ash from the water outlet and returning the ash to the fixed bed gasifier (1); a slag pool pump is arranged on a pipeline from the slag pool (21) to the fixed bed gasifier (1).
8. The fixed bed gasification system according to any one of claims 1 to 7, wherein the fixed bed gasification furnace (1) is provided with a water cooled wall; the lower part and the upper part of the shell of the fixed bed gasifier (1) are respectively provided with a boiler water inlet and a boiler water outlet, and are used for leading in boiler water from the boiler water inlet and carrying out heat exchange and temperature rise with the water cooling wall to form a steam-water mixture and outputting the steam-water mixture from the boiler water outlet;
preferably, the fixed bed gasification system further comprises a steam drum (22), wherein the steam drum (22) is respectively provided with a steam inlet, a water outlet and a steam outlet, the steam inlet is connected to a boiler water outlet of the fixed bed gasification furnace (1), the water outlet is connected to a boiler water inlet of the fixed bed gasification furnace (1), the steam outlet is connected to the gasifying agent inlet (102) and is used for introducing a steam-water mixture from the fixed bed gasification furnace (1) from the steam inlet to perform steam-water separation, water is output from the water outlet and circulated into a shell of the fixed bed gasification furnace (1), and steam is output from the steam outlet to a furnace core in the fixed bed gasification furnace (1) to be used as the gasifying agent;
A boiler water circulation pump (23) is arranged on a pipeline from a water outlet of the steam drum (22) to a boiler water inlet of the fixed bed gasifier (1) and is used for pumping the water circulation from the steam drum (22) to a shell of the fixed bed gasifier (1).
9. A fixed bed gasification process, characterized in that it is carried out with a fixed bed gasification system according to any one of claims 1 to 8.
10. The fixed bed gasification process of claim 9, wherein the fixed bed gasification process comprises:
(1) Introducing a carbonaceous raw material and a gasifying agent into the fixed bed gasifier (1) respectively to perform chemical reaction, discharging ash, and self-discharging a mixture containing CH 4 、CO、CO 2 、H 2 And steam and carrying crude product gas of oil, phenol, ammonia and dust;
(2) Introducing the obtained crude product gas into a scrubber (2), performing chilling washing by using the introduced liquid washing oil to remove part of dust and oil in the crude product gas, and outputting an oil-gas mixture;
(3) Introducing the obtained oil-gas mixture into the oil washing tower (3), performing chilling washing by using the introduced liquid washing oil, and then performing gas-liquid separation to output dust-containing oil containing dust and phenol and CH-containing oil 4 、CO、CO 2 And H 2 And the gas carrying ammonia and water vapor is used as the product gas.
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