CN112239678A - Pulverized coal hydro-gasification system and process method thereof - Google Patents
Pulverized coal hydro-gasification system and process method thereof Download PDFInfo
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- CN112239678A CN112239678A CN202010737674.5A CN202010737674A CN112239678A CN 112239678 A CN112239678 A CN 112239678A CN 202010737674 A CN202010737674 A CN 202010737674A CN 112239678 A CN112239678 A CN 112239678A
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- 239000003245 coal Substances 0.000 title claims abstract description 282
- 238000002309 gasification Methods 0.000 title claims abstract description 115
- 238000000034 method Methods 0.000 title claims abstract description 32
- 230000008569 process Effects 0.000 title claims abstract description 22
- 239000007789 gas Substances 0.000 claims abstract description 103
- 238000011084 recovery Methods 0.000 claims abstract description 66
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 48
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 48
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 43
- 239000001257 hydrogen Substances 0.000 claims abstract description 43
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 43
- 238000006243 chemical reaction Methods 0.000 claims abstract description 39
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 20
- 239000001301 oxygen Substances 0.000 claims abstract description 20
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 20
- 239000007788 liquid Substances 0.000 claims abstract description 6
- 239000000463 material Substances 0.000 claims description 62
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 32
- 239000003034 coal gas Substances 0.000 claims description 27
- 239000000203 mixture Substances 0.000 claims description 18
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 18
- 238000007599 discharging Methods 0.000 claims description 16
- 229910052757 nitrogen Inorganic materials 0.000 claims description 15
- 239000002994 raw material Substances 0.000 claims description 15
- 239000007787 solid Substances 0.000 claims description 15
- 238000000926 separation method Methods 0.000 claims description 9
- 238000002156 mixing Methods 0.000 claims description 2
- 244000188595 Brassica sinapistrum Species 0.000 claims 1
- 235000004977 Brassica sinapistrum Nutrition 0.000 claims 1
- 239000002245 particle Substances 0.000 claims 1
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 abstract description 27
- 238000004519 manufacturing process Methods 0.000 abstract description 6
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 abstract description 5
- 229910052799 carbon Inorganic materials 0.000 abstract description 5
- 238000001816 cooling Methods 0.000 abstract description 5
- 230000008901 benefit Effects 0.000 abstract description 3
- 238000000746 purification Methods 0.000 abstract description 3
- 238000005984 hydrogenation reaction Methods 0.000 description 7
- 238000000197 pyrolysis Methods 0.000 description 5
- 230000035484 reaction time Effects 0.000 description 5
- 230000009471 action Effects 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 238000010438 heat treatment Methods 0.000 description 4
- 239000000843 powder Substances 0.000 description 4
- 230000004888 barrier function Effects 0.000 description 3
- 239000002918 waste heat Substances 0.000 description 3
- 230000006978 adaptation Effects 0.000 description 2
- 229910001873 dinitrogen Inorganic materials 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 239000000571 coke Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 239000003209 petroleum derivative Substances 0.000 description 1
- 238000011027 product recovery Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 239000002893 slag Substances 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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Classifications
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/48—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
- C10J3/46—Gasification of granular or pulverulent flues in suspension
-
- 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
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/48—Apparatus; Plants
- C10J3/50—Fuel charging devices
-
- 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
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/48—Apparatus; Plants
- C10J3/52—Ash-removing devices
-
- 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
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2200/00—Details of gasification apparatus
- C10J2200/15—Details of feeding means
- C10J2200/152—Nozzles or lances for introducing gas, liquids or suspensions
-
- 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
- C10J2300/0936—Coal fines for producing producer gas
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0953—Gasifying agents
- C10J2300/0959—Oxygen
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- 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
- C10J2300/0966—Hydrogen
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
- C10J2300/1807—Recycle loops, e.g. gas, solids, heating medium, water
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention discloses a pulverized coal hydro-gasification system and a process method thereof, wherein the system comprises a gasification furnace, a heat energy recovery device, a pulverized coal feeding system, a cyclone separator and a pulverized coal pressurizing system; the method comprises the following steps: sending pulverized coal, heated hydrogen and oxygen into a gasification furnace through a gasification furnace nozzle; carrying out hydro-gasification reaction; and (4) exchanging heat, and directly cooling and separating the separated synthesis gas to obtain a gas product and a liquid oil product. Has the advantages that: the hydro-gasification system has simple connection structure and is easy to realize; the hydro-gasification system is simplified, and further the hydro-gasification process flow is simplified; and the purification efficiency of the synthesis gas is improved; the content of methane in the synthesis gas is effectively increased; the carbon conversion rate of the pulverized coal is improved, the consumption of oxygen and hydrogen is greatly reduced, the energy is saved, and the production cost is reduced.
Description
The technical field is as follows:
the invention belongs to the field of pulverized coal processing, and particularly relates to a pulverized coal hydro-gasification system and a process method thereof.
Background art:
coal plays an important role in the world energy composition, and petroleum and natural gas resources in China are not rich enough, but coal resources are sufficient, so that in an energy consumption structure, the coal resources always have a large proportion (about 70 percent) and cannot be changed for a long time in the future; in recent years, a process for extracting tar and gas products from raw coal by coal pyrolysis and hydro-gasification has been receiving more and more attention.
The hydro-gasification refers to a process that hydrogen, oxygen and coal powder react in a gasification furnace at medium temperature (700-.
Semicoke and synthesis gas produced after reaction in the gasification furnace downwards enter a semicoke collecting section and then are subjected to gas-solid separation, the produced synthesis gas needs to be subjected to gas-solid separation through a two-stage cyclone separator and then is subjected to heat energy recovery through a waste heat boiler, and the cooled synthesis gas is filtered and purified through a crude gas filter and then is sent to an oil product recovery section; and the solid semicoke filtered by the cyclone air separator and the crude gas filter and the high-temperature semicoke produced in the gasifier enter a semicoke cooler through a coke discharge pipe at the bottom of the gasifier for cooling, and the cooled semicoke is discharged after being depressurized by a lock hopper slag discharge system.
The adoption of the hydrogenation system and the hydrogenation process has the following problems:
1. after the coal powder enters the gasification furnace through the lock hopper system, the coal powder undergoes a hydropyrolysis reaction, and the equation for generating methane by the reaction is as follows:
CV+H→CH4，C++H→CH4；C++C+→C-；C-+H→CH4；
the reaction of the hydrocarbons is incomplete due to the short reaction time in the gasifier, CH4The content is slightly low;
2. the generated semicoke and synthesis gas need to be subjected to heat exchange and temperature reduction through a water-cooling heat exchanger, so that the recovery and utilization rate of the semicoke and the synthesized heat energy is low, and the waste of the heat energy is caused; the amount of high-temperature hydrogen and oxygen which provide heat energy in the gasification furnace is increased, so that energy is wasted, and the production cost is increased;
3. the semicoke is easy to be entrained by gas due to the specific characteristics of looseness, porosity and low density; and the removal of the semicoke in the synthesis gas in the later period is very difficult, so that a process flow and a large amount of equipment are required to be added in the subsequent process of removing the semicoke in the synthesis gas, the operation is complex, and the cost is high.
The invention content is as follows:
the first purpose of the invention is to provide a pulverized coal hydro-gasification system which has simple connection structure and simplifies the system.
The second purpose of the invention is to provide a pulverized coal gasification process method which realizes heat energy recovery and improves the methane content.
The technical scheme of the invention discloses a pulverized coal hydro-gasification system which comprises a gasification furnace, a heat energy recovery device, a pulverized coal feeding system, a cyclone separator and a pulverized coal pressurizing system;
the gas outlet of the gasification furnace is communicated with the gas inlet of the heat energy recovery device; the discharge hole of the pulverized coal feeding system is communicated with the feed hole of the heat energy recovery device;
the air outlet of the heat energy recovery device is communicated with the air inlet of the cyclone separator; the discharge hole of the heat energy recovery device and the discharge hole of the cyclone separator are both communicated with the feed inlet of the pulverized coal pressurizing system;
and the discharge holes of the pulverized coal pressurizing system and the pulverized coal charging system are communicated with the feed hole of the gasification furnace.
Further, it also includes a semicoke discharge system; and the discharge port of the gasification furnace is communicated with the feed inlet of the semicoke discharging system.
Furthermore, the pulverized coal charging system comprises a pulverized coal bunker, a pulverized coal normal pressure tank, a variable pressure lock hopper, a pulverized coal charging bucket, a hydrogen source, a nitrogen source, a pulverized coal filter and a torch burner;
the discharge hole of the pulverized coal bunker is communicated with the feed inlet of the pulverized coal normal pressure tank; the discharge hole of the pulverized coal normal pressure tank is communicated with the feed inlet of the pressure-variable lock hopper; the discharge hole of the pressure swing lock hopper is communicated with the feed inlet of the pulverized coal material sending tank; the discharge hole of the pulverized coal material sending tank is respectively communicated with the gasification furnace and the feed hole of the heat energy recovery device;
the hydrogen source and the nitrogen source are both communicated with an air inlet of the pressure swing lock hopper; the air outlet of the variable pressure lock hopper is communicated with the air inlet of the pulverized coal filter; the gas outlet of the pulverized coal filter is communicated with the gas inlet of the torch burner;
a first balance pipe is communicated between the variable pressure lock hopper and the pulverized coal material dispensing tank.
Further, a discharge pipe is arranged at a discharge port of the pulverized coal material dispensing tank, and one end of the discharge pipe is communicated with the discharge port of the pulverized coal material dispensing tank; the other end of the discharge pipe is communicated with a feed delivery pipe, and one end of the feed delivery pipe is communicated with the hydrogen source; the other end of the conveying pipe is respectively communicated with the gasification furnace and the feed inlet of the heat energy recovery device.
Furthermore, the pulverized coal pressurizing system comprises a pulverized coal collecting tank, a pulverized coal lock hopper, an intermediate material sending tank, a coal gas source, a high-temperature filter and a torch burner;
the heat energy recovery device and the discharge hole of the cyclone separator are communicated with the feed inlet of the pulverized coal collecting tank; the discharge hole of the pulverized coal collecting tank is communicated with the feed inlet of the pulverized coal locking hopper, and the discharge hole of the pulverized coal locking hopper is communicated with the feed inlet of the middle material sending tank; the discharge hole of the intermediate material sending tank is communicated with the feed hole of the gasification furnace;
the coal gas source is communicated with the gas inlet of the pulverized coal lock hopper; the gas outlet of the pulverized coal lock hopper is communicated with the gas inlet of the high-temperature filter, and the gas outlet of the high-temperature filter is communicated with the gas inlet of the torch burner;
a second balance pipe is communicated and arranged between the pulverized coal lock hopper and the pulverized coal collecting tank; and a third balance pipe is communicated between the pulverized coal lock hopper and the middle material sending tank.
Further, the semicoke discharging system comprises a semicoke cooler, a semicoke collecting tank, a semicoke lock hopper, a semicoke water cooler, a semicoke storage bin, a coal gas source, a nitrogen source, a semicoke filter and a torch burner;
the discharge hole of the gasification furnace is communicated with the feed inlet of the semicoke cooler; the discharge hole of the semicoke cooler is communicated with the feed inlet of the semicoke collecting tank; the discharge hole of the semicoke collecting tank is communicated with the feed inlet of the semicoke locking hopper; the discharge hole of the semicoke lock hopper is communicated with the feed inlet of the semicoke water cooler; the discharge hole of the semicoke water cooler is communicated with the feed inlet of the semicoke storage bin;
the coal gas source is respectively communicated with the semicoke cooler and the air inlet of the semicoke lock hopper; the nitrogen source is communicated with an air inlet of the semicoke lock hopper;
the air outlet of the semicoke lock hopper is communicated with the air inlet of the semicoke filter; the gas outlet of the semicoke filter is communicated with the gas inlet of the torch burner;
and the semicoke lock hopper is communicated with the semicoke collecting tank through a fourth balance pipe.
Further, the heat energy recovery device comprises a tower body; a plurality of nozzles forming an included angle of 45-90 degrees with the center line of the tower body are uniformly arranged above the inside of the tower body;
the top of the tower body is provided with an air outlet, the side wall of the tower body below the nozzle is provided with an air inlet, and the bottom of the tower body is provided with a discharge hole.
The invention also discloses a pulverized coal gasification process method, which comprises the following steps:
step 1: sending pulverized coal, heated hydrogen and oxygen into a gasification furnace through a gasification furnace nozzle;
step 2: mixing the pulverized coal in the step 1 with the heated hydrogen and oxygen in a reaction section in the gasification furnace, and carrying out hydro-gasification reaction to generate semicoke and synthesis gas;
and step 3: the pulverized coal in the step 1 and the synthesis gas containing a small amount of semicoke in the step 2 enter a heat energy recovery device for heat exchange, the pulverized coal intercepts the semicoke in the synthesis gas during the heat exchange to obtain a high-temperature mixture, and the high-temperature mixture is deposited at the bottom of the heat energy recovery device; the synthetic gas enters a cyclone separator for gas-solid separation, and the separated synthetic gas is directly cooled and separated to obtain a gas product and a liquid oil product;
and 4, step 4: and 3, conveying the high-temperature mixture obtained in the step 3 and the solid separated by the cyclone separator serving as raw materials to a gasification furnace through a pulverized coal pressurizing system.
Further, the semicoke in the step 2 is discharged from the gasification furnace and cooled and depressurized through a semicoke discharging system to obtain a semicoke product.
Further, the granularity of the pulverized coal in the step 1 is 5-90 μm, and the water content is less than 5%; the temperature of the hydrogen is 450 ℃ at the lowest; the feed temperature in step 4 was a minimum of 300 ℃.
Further, the conveying pressure of the pulverized coal in the step 1 and the step 2 is 7.6Mpa +/-0.2; the conveying pressure of the raw materials in the step 4 is 7.6Mpa +/-0.2.
Further, the reaction temperature in the gasification furnace in the step 2 is 700-.
Further, the temperature in the heat energy recovery device in the step 3 is 750-850 ℃, and the pressure is 6.9 Mpa.
The invention has the advantages that:
1. the hydro-gasification system has simple connection structure and is easy to realize; the pulverized coal exchanges heat with the high-temperature synthesis gas obtained by reaction in the heat energy recovery device, the semicoke which is difficult to separate from the synthesizer is intercepted by a pulverized coal barrier formed in the heat energy recovery device, the cyclone separator separates the rest pulverized coal in the synthesis gas, and the separation efficiency is about more than 98 percent, so that the separated synthesis gas can be directly cooled and separated, two-stage cyclone separators, waste heat boilers and crude gas filters are not needed, the treatment equipment is reduced, the hydro-gasification system is simplified, and the hydro-gasification process flow is simplified; and the purification efficiency of the synthesis gas is improved;
2. in the invention, the pulverized coal exchanges heat with the high-temperature synthesis gas obtained by reaction in the heat energy recovery device, and partial volatile matters with stronger activity in the pulverized coal are extracted by pyrolysis under the action of high temperature, so that the content of methane in the synthesis gas is effectively increased; the high-temperature pulverized coal directly reacts with high-temperature hydrogen in the gasification furnace without heating the pulverized coal, so that the reaction time is increased, the carbon conversion rate of the pulverized coal is improved, and the methane content can be improved by about 2% at least according to the conventional gasified hydrogen-coal ratio of 0.3;
3. the temperature of the pulverized coal after heat exchange in the heat energy recovery device is more than or equal to 300 ℃, so that heat energy recovery is realized; the high-temperature pulverized coal enters a reaction section in the gasification furnace to participate in hydrogenation reaction, so that the consumption of oxygen and hydrogen is greatly reduced, the energy is saved, and the production cost is reduced.
Description of the drawings:
fig. 1 is a schematic overall structure diagram of an embodiment of the present invention.
The device comprises a gasification furnace 1, a heat energy recovery device 2, a tower body 2.1, a nozzle 2.2, a pulverized coal feeding system 3, a pulverized coal bunker 3.1, a pulverized coal normal pressure tank 3.2, a variable pressure lock hopper 3.3, a pulverized coal sending tank 3.4, a hydrogen source 3.5, a pulverized coal filter 3.6, a first balance pipe 3.7, a discharging pipe 3.8, a conveying pipe 3.9, a cyclone separator 4, a pulverized coal pressurizing system 5, a pulverized coal collecting tank 5.1, a pulverized coal lock hopper 5.2, an intermediate sending tank 5.3, a high-temperature filter 5.4, a second balance pipe 5.5, a third balance pipe 5.6, a semicoke discharging system 6, a semicoke cooler 6.1, a semicoke collecting tank 6.2, a semicoke lock hopper 6.3, a semicoke water cooler 6.4, a semicoke bunker 6.5, a semicoke filter 6.6, a fourth balance pipe 6.7, a coal storage source 7, a nitrogen source 8 and a torch burner 9.
The specific implementation mode is as follows:
the present invention will be described in further detail by way of examples with reference to the accompanying drawings.
Example 1: as shown in fig. 1, a pulverized coal hydro-gasification system comprises a gasification furnace 1, a heat energy recovery device 2, a pulverized coal charging system 3, a cyclone separator 4, a pulverized coal pressurizing system 5 and a semicoke discharging system 6; the gas outlet of the gasification furnace 1 is communicated with the gas inlet of the heat energy recovery device 2; a discharge hole of the pulverized coal feeding system 3 is communicated with a feed inlet of the heat energy recovery device 2; the air outlet of the heat energy recovery device 2 is communicated with the air inlet of the cyclone separator 4; the discharge hole of the heat energy recovery device 2 and the discharge hole of the cyclone separator 4 are both communicated with the feed inlet of the pulverized coal pressurizing system 5; the discharge ports of the pulverized coal pressurizing system 5 and the pulverized coal charging system 3 are communicated with the feed port of the gasification furnace 1; the discharge port of the gasification furnace 1 is communicated with the feed port of the semicoke discharge system 6.
The pulverized coal charging system 3 comprises a pulverized coal bunker 3.1, a pulverized coal normal pressure tank 3.2, a variable pressure lock hopper 3.3, a pulverized coal charging bucket 3.4, a hydrogen source 3.5, a nitrogen source 8, a pulverized coal filter 3.6 and a torch burner 9; a discharge hole of the pulverized coal bunker 3.1 is communicated with a feed inlet of the pulverized coal atmospheric tank 3.2; a discharge hole of the pulverized coal normal pressure tank 3.2 is communicated with a feed inlet of the pressure-variable lock hopper 3.3; the discharge hole of the pressure swing lock hopper 3.3 is communicated with the feed inlet of the pulverized coal material sending tank 3.4; the discharge hole of the pulverized coal material sending tank 3.4 is respectively communicated with the feed holes of the gasification furnace 1 and the heat energy recovery device 2; the hydrogen source 3.5 and the nitrogen source 8 are both communicated with the air inlet of the pressure swing lock hopper 3.3; the air outlet of the pressure-changing lock hopper 3.3 is communicated with the air inlet of the pulverized coal filter 3.6; the gas outlet of the coal powder filter 3.6 is communicated with the gas inlet of the torch burner 9; a first balance pipe 3.7 is communicated between the pressure swing lock hopper 3.3 and the pulverized coal material sending tank 3.4.
A discharge pipe 3.8 is arranged at a discharge port of the pulverized coal material dispensing tank 3.4, and one end of the discharge pipe 3.8 is communicated with the discharge port of the pulverized coal material dispensing tank 3.4; the other end of the discharge pipe 3.8 is communicated with a feed delivery pipe 3.9, and one end of the feed delivery pipe 3.9 is communicated with a hydrogen source 3.5; the other end of the material conveying pipe 3.9 is respectively communicated with the feed inlets of the gasification furnace 1 and the heat energy recovery device 2.
During the fine coal ordinary pressure jar 3.2 was sent to fine coal ordinary pressure jar to the fine coal in the fine coal feed bin 3.1, when the charge level reached the highest material level in fine coal ordinary pressure jar 3.2, stopped carrying fine coal to in the vary voltage lock fill 3.3 beginning to carry the fine coal in the fine coal ordinary pressure jar 3.2, when the charge level reached minimum material level in fine coal ordinary pressure jar 3.2, stopped carrying the material in the vary voltage lock fill 3.3, and send the fine coal in the fine coal feed bin 3.1 to in the fine coal ordinary pressure jar 3.2.
After the pulverized coal is sent to the pressure swing lock hopper 3.3, the hydrogen gas charging is started to be introduced into the pressure swing lock hopper 3.3, when the pressure in the pressure swing lock hopper 3.3 is the same as the pressure in the pulverized coal sending tank 3.4, the hydrogen gas charging is stopped, a valve on a first balance pipe 3.7 is opened, the pressure swing lock hopper 3.3 is communicated with the pulverized coal sending tank 3.4, then the pulverized coal in the pressure swing lock hopper 3.3 starts to be conveyed into the pulverized coal sending tank 3.4, when the material level in the pulverized coal sending tank 3.4 reaches the highest value, the conveying is stopped, the valve on the first balance pipe 3.7 is closed, then the nitrogen gas is introduced into the pressure swing lock hopper 3.3, the hydrogen gas in the pressure swing lock hopper 3.3 is replaced and discharged to a torch burner 9 for combustion, after the replacement is finished, the nitrogen gas introduction is stopped, the gas in the pressure swing lock hopper 3.3 is discharged, the gas discharge is stopped after the pressure is discharged to the normal pressure, and the gas in the pressure swing lock hopper 3.4 is conveyed into the pressure swing.
When the material level in the pulverized coal material sending tank 3.4 reaches the highest value, the reaction just starts to transmit the pulverized coal gas in the pulverized coal material sending tank 3.4 to the gasification furnace 1 and the heat energy recovery device 2 through hydrogen, and after the pulverized coal with the heat energy recovered is transmitted to the gasification furnace 1 through the pulverized coal pressurization system 5, the pulverized coal in the pulverized coal material sending tank 3.4 is stopped being directly transmitted to the gasification furnace 1; when the material level in the pulverized coal material sending tank 3.4 reaches the lowest value, hydrogen is introduced into the variable pressure lock hopper 3.3 for pressurizing, when the pressure in the variable pressure lock hopper 3.3 is the same as the pressure in the pulverized coal material sending tank 3.4, the hydrogen pressurizing is stopped, the valve on the first balance pipe 3.7 is opened, the variable pressure lock hopper 3.3 is communicated with the pulverized coal material sending tank 3.4, then the pulverized coal in the variable pressure lock hopper 3.3 begins to be conveyed into the pulverized coal material sending tank 3.4, and the pulverized coal conveying and feeding are realized by adopting the mode.
The pulverized coal pressurizing system 5 comprises a pulverized coal collecting tank 5.1, a pulverized coal lock hopper 5.2, an intermediate feeding tank 5.3, a coal gas source 7, a high-temperature filter 5.4 and a torch burner 9;
the discharge ports of the heat energy recovery device 2 and the cyclone separator 4 are communicated with the feed inlet of the pulverized coal collecting tank 5.1; a discharge hole of the pulverized coal collecting tank 5.1 is communicated with a feed inlet of the pulverized coal locking hopper 5.2, and a discharge hole of the pulverized coal locking hopper 5.2 is communicated with a feed inlet of the intermediate feeding tank 5.3; the discharge hole of the middle material sending tank 5.3 is communicated with the feed hole of the gasification furnace 1;
the coal gas source 7 is communicated with the gas inlet of the pulverized coal lock hopper 5.2; the gas outlet of the pulverized coal lock hopper 5.2 is communicated with the gas inlet of the high-temperature filter 5.4, and the gas outlet of the high-temperature filter 5.4 is communicated with the gas inlet of the torch burner 9;
a second balance pipe 5.5 is communicated between the pulverized coal lock 5.2 and the pulverized coal collecting tank 5.1; a third balance pipe 5.6 is communicated between the pulverized coal lock 5.2 and the intermediate feeding tank 5.3.
The high-temperature mixture in the heat energy recovery device 2 and the solid separated by the cyclone separator 4 are sent to the pulverized coal collecting tank 5.1, when the material level in the pulverized coal collecting tank 5.1 reaches the highest material level, the material conveying is stopped, the pulverized coal in the pulverized coal collecting tank 5.1 is conveyed to the pulverized coal locking bucket 5.2 with the same pressure, when the material level in the pulverized coal collecting tank 5.1 reaches the lowest material level, the material conveying to the pulverized coal locking bucket 5.2 is stopped, and the high-temperature mixture in the heat energy recovery device 2 and the solid separated by the cyclone separator 4 are sent to the pulverized coal collecting tank 5.1.
After the material is sent to the pulverized coal lock hopper 5.2, a small amount of coal gas is introduced into the pulverized coal lock hopper 5.2 for pressurizing, when the pressure in the pulverized coal lock hopper 5.2 is the same as the pressure in the middle sending tank 5.3, the coal gas pressurizing is stopped, a valve on a third balance pipe 5.6 is opened, the pulverized coal lock hopper 5.2 is communicated with the middle sending tank 5.3, then the pulverized coal in the pulverized coal lock hopper 5.2 starts to be sent into the middle sending tank 5.3, when the material level in the middle sending tank 5.3 reaches the highest value, the sending is stopped, the valve on the third balance pipe 5.6 is closed, then the hydrogen in the pulverized coal lock hopper 5.2 is discharged to a torch burner 9 for burning treatment, until the pressure in the lock hopper 5.2 is the same as the pressure in the pulverized coal collecting tank 5.1, the discharging of the coal gas is stopped, then the valve on the second balance pipe 5.5 is opened, the pulverized coal lock hopper 5.2 is communicated with the pulverized coal collecting tank 5.1, and the conveying in the collecting tank 5.1 is started, when the material level in the pulverized coal collecting tank 5.1 reaches the lowest material level, stopping conveying the materials into the pulverized coal lock hopper 5.2, closing a valve on the second balance pipe 5.5, and starting introducing a small amount of coal gas into the pulverized coal lock hopper 5.2 for pressurizing.
When the material level in the intermediate material sending tank 5.3 reaches the highest value, the material in the intermediate material sending tank 5.3 is used as a raw material and is conveyed to the gasification furnace 1 to participate in hydrogenation reaction; when the material level in the middle material sending tank 5.3 reaches the lowest value, a small amount of coal gas is introduced into the fine coal locking hopper 5.2 for pressurizing, when the pressure in the fine coal locking hopper 5.2 is the same as the pressure in the middle material sending tank 5.3, the coal gas pressurizing is stopped, the valve on the third balance pipe 5.6 is opened, the fine coal locking hopper 5.2 is communicated with the middle material sending tank 5.3, the material in the fine coal locking hopper 5.2 begins to be conveyed into the middle material sending tank 5.3, and the high-temperature material after heat exchange is conveyed to the gasification furnace 1 by adopting the mode.
The semicoke discharging system 6 comprises a semicoke cooler 6.1, a semicoke collecting tank 6.2, a semicoke lock hopper 6.3, a semicoke water cooler 6.4, a semicoke storage bin 6.5, a coal gas source 7, a nitrogen source 8, a semicoke filter 6.6 and a torch burner 9; the discharge hole of the gasification furnace 1 is communicated with the feed inlet of the semicoke cooler 6.1; a discharge hole of the semicoke cooler 6.1 is communicated with a feed hole of the semicoke collecting tank 6.2; a discharge hole of the semicoke collecting tank 6.2 is communicated with a feed hole of the semicoke lock hopper 6.3; the discharge hole of the semicoke lock hopper 6.3 is communicated with the feed inlet of the semicoke water cooler 6.4; the discharge hole of the semicoke water cooler 6.4 is communicated with the feed inlet of the semicoke storage bin 6.5; the coal gas source 7 is respectively communicated with the gas inlets of the semicoke cooler 6.1 and the semicoke lock hopper 6.3; the nitrogen source 8 is communicated with the air inlet of the semicoke lock hopper 6.3; the air outlet of the semicoke lock hopper 6.3 is communicated with the air inlet of the semicoke filter 6.6; the gas outlet of the semicoke filter 6.6 is communicated with the gas inlet of the torch burner 9; the semicoke lock hopper 6.3 is communicated with the semicoke collecting tank 6.2 through a fourth balance pipe 6.7.
The semicoke at the bottom of the gasification furnace 1 is sent to a semicoke cooler 6.1, and the semicoke is conveyed to a semicoke collecting tank 6.2 while introducing coal gas from the bottom of the semicoke cooler 6.1 for cooling the semicoke, when the material level in the semicoke collecting tank 6.2 reaches the highest material level, stopping introducing semicoke and coal gas into the semicoke cooler 6.1, simultaneously, coal gas is pumped into the semicoke lock hopper 6.3 for pressurizing, when the pressure in the semicoke lock hopper 6.3 is the same as the pressure in the semicoke collecting tank 6.2, stopping pressurizing the coal gas, opening a valve on the fourth balance pipe 6.7 to communicate the semicoke collecting tank 6.2 with the semicoke lock hopper 6.3, then the pulverized coal in the semicoke collecting tank 6.2 is conveyed to the semicoke lock hopper 6.3, when the material level in the semicoke collecting tank 6.2 reaches the lowest material level, stopping conveying the materials into the semicoke lock hopper 6.3, closing the valve on the fourth balance pipe 6.7 and starting to feed semicoke and coal gas into the semicoke cooler 6.1.
After the semicoke is sent to a semicoke lock hopper 6.3, introducing nitrogen into the semicoke lock hopper 6.3, replacing and discharging coal gas in the semicoke lock hopper 6.3 to a torch burner 9 for burning treatment, after replacement, stopping introducing the nitrogen, discharging and decompressing the gas in the semicoke lock hopper 6.3, after discharging to normal pressure, stopping discharging the gas, conveying the semicoke in the semicoke lock hopper 6.3 to a semicoke water cooler 6.4 for heat exchange with cooling water, discharging the semicoke in a semicoke storage bin 6.5 for storage after heat exchange, and finally recovering raw materials and the like which are used for producing coal water slurry; after the semicoke in the semicoke lock hopper 6.3 is discharged, closing a valve between the semicoke lock hopper 6.3 and the semicoke water cooler 6.4; and then, introducing coal gas into the semicoke lock hopper 6.3 for pressurizing, stopping the coal gas pressurizing when the pressure in the semicoke lock hopper 6.3 is the same as that of the semicoke collecting tank 6.2, opening a valve on a fourth balance pipe 6.7 to communicate the semicoke collecting tank 6.2 with the semicoke lock hopper 6.3, and then conveying the pulverized coal in the semicoke collecting tank 6.2 into the semicoke lock hopper 6.3 to realize the cooling and discharging of the semicoke.
The heat energy recovery device 2 comprises a tower body 2.1; a plurality of nozzles 2.2 which form an included angle of 45-90 degrees with the central line of the tower body 2.1 are uniformly arranged above the inside of the tower body 2.1; ensuring that atomized pulverized coal sprayed by a nozzle 2.2 in the tower body 2.1 forms a pulverized coal barrier, so that semicoke in the synthesis gas is fully contacted with the pulverized coal, and the semicoke is intercepted from the synthesis gas; an air outlet is arranged at the top of the tower body 2.1, an air inlet is arranged on the side wall of the tower body 2.1 below the nozzle 2.2, and a discharge hole is arranged at the bottom of the tower body 2.1.
The hydro-gasification system has simple connection structure and is easy to realize; the pulverized coal exchanges heat with the high-temperature synthesis gas obtained by reaction in the heat energy recovery device 2, the semicoke which is difficult to separate from the synthesizer is intercepted by a pulverized coal barrier formed in the heat energy recovery device 2, the cyclone separator 4 separates the rest pulverized coal in the synthesis gas, and the separation efficiency is about more than 98 percent, so that the separated synthesis gas can be directly cooled and separated, two stages of cyclone separators 4, waste heat boilers and crude gas filters are not needed, the treatment equipment is reduced, the hydro-gasification system is simplified, and the hydro-gasification process flow is simplified; and the purification efficiency of the synthesis gas is improved.
Example 2: a pulverized coal gasification process utilizing the system of example 1, comprising the steps of:
step 1: sending pulverized coal, heated hydrogen and oxygen into a gasification furnace 1 through a nozzle 2.2 of the gasification furnace 1; the granularity of the pulverized coal is 5-90 mu m, the water content is less than 5 percent, and the conveying pressure is 7.4 Mpa; the temperature of the hydrogen is 450 ℃ at the lowest;
step 2: the pulverized coal in the step 1 is mixed with the heated hydrogen and oxygen in a reaction section in the gasification furnace 1, and a hydro-gasification reaction is carried out to generate semicoke and synthesis gas; the semicoke is discharged by the gasification furnace 1 and is cooled and depressurized by a semicoke discharge system 6 to obtain a semicoke product; the reaction temperature in the gasification furnace 1 is 700 ℃, and the reaction pressure is 7.0 Mpa.
And step 3: the pulverized coal in the step 1 and the synthesis gas containing a small amount of semicoke in the step 2 enter a heat energy recovery device 2 for heat exchange, the pulverized coal intercepts the semicoke in the synthesis gas during the heat exchange to obtain a high-temperature mixture, and the high-temperature mixture is deposited at the bottom of the heat energy recovery device 2; the synthesis gas enters a cyclone separator 4 for gas-solid separation, and the separated synthesis gas is directly cooled and separated to obtain a gas product and a liquid oil product; the temperature in the heat recovery device 2 is 750 ℃ and the pressure is 6.9 Mpa.
And 4, step 4: the high-temperature mixture in the step 3 and the solid separated by the cyclone separator 4 are taken as raw materials and are conveyed into the gasification furnace 1 through a pulverized coal pressurizing system 5, and the lowest temperature of the raw materials is 300 ℃; the conveying pressure of the raw material was 7.4 MPa.
In the invention, the pulverized coal exchanges heat with the high-temperature synthesis gas obtained by reaction in the heat energy recovery device 2, and partial volatile matters with stronger activity in the pulverized coal are extracted by pyrolysis under the action of high temperature, so that the content of methane in the synthesis gas is effectively increased; the high-temperature pulverized coal directly reacts with high-temperature hydrogen in the gasification furnace 1 without heating the pulverized coal, so that the reaction time is increased, the carbon conversion rate of the pulverized coal is improved, and the methane content can be improved by about 2% at least according to the conventional gasified hydrogen-coal ratio of 0.3; the temperature of the pulverized coal after heat exchange in the heat energy recovery device 2 is more than or equal to 300 ℃, so that heat energy recovery is realized; high-temperature pulverized coal enters a reaction section in the gasification furnace 1 to participate in hydrogenation reaction, so that the consumption of oxygen and hydrogen is greatly reduced, the energy is saved, and the production cost is reduced.
Example 3: a pulverized coal gasification process utilizing the system of example 1, comprising the steps of:
step 1: sending pulverized coal, heated hydrogen and oxygen into a gasification furnace 1 through a nozzle 2.2 of the gasification furnace 1; the granularity of the pulverized coal is 5-90 mu m, the water content is less than 5 percent, and the conveying pressure is 7.6 Mpa; the temperature of the hydrogen is 450 ℃ at the lowest;
step 2: the pulverized coal in the step 1 is mixed with the heated hydrogen and oxygen in a reaction section in the gasification furnace 1, and a hydro-gasification reaction is carried out to generate semicoke and synthesis gas; the semicoke is discharged by the gasification furnace 1 and is cooled and depressurized by a semicoke discharge system 6 to obtain a semicoke product; the reaction temperature in the gasification furnace 1 is 800 ℃, and the reaction pressure is 7.0 Mpa.
And step 3: the pulverized coal in the step 1 and the synthesis gas containing a small amount of semicoke in the step 2 enter a heat energy recovery device 2 for heat exchange, the pulverized coal intercepts the semicoke in the synthesis gas during the heat exchange to obtain a high-temperature mixture, and the high-temperature mixture is deposited at the bottom of the heat energy recovery device 2; the synthesis gas enters a cyclone separator 4 for gas-solid separation, and the separated synthesis gas is directly cooled and separated to obtain a gas product and a liquid oil product; the temperature in the heat recovery device 2 is 800 ℃ and the pressure is 6.9 Mpa.
And 4, step 4: the high-temperature mixture in the step 3 and the solid separated by the cyclone separator 4 are taken as raw materials and are conveyed into the gasification furnace 1 through a pulverized coal pressurizing system 5, and the lowest temperature of the raw materials is 300 ℃; the conveying pressure of the raw material was 7.6 MPa.
In the invention, the pulverized coal exchanges heat with the high-temperature synthesis gas obtained by reaction in the heat energy recovery device 2, and partial volatile matters with stronger activity in the pulverized coal are extracted by pyrolysis under the action of high temperature, so that the content of methane in the synthesis gas is effectively increased; the high-temperature pulverized coal directly reacts with high-temperature hydrogen in the gasification furnace 1 without heating the pulverized coal, so that the reaction time is increased, the carbon conversion rate of the pulverized coal is improved, and the methane content can be improved by about 2% at least according to the conventional gasified hydrogen-coal ratio of 0.3; the temperature of the pulverized coal after heat exchange in the heat energy recovery device 2 is more than or equal to 300 ℃, so that heat energy recovery is realized; high-temperature pulverized coal enters a reaction section in the gasification furnace 1 to participate in hydrogenation reaction, so that the consumption of oxygen and hydrogen is greatly reduced, the energy is saved, and the production cost is reduced.
Example 4: a pulverized coal gasification process utilizing the system of example 1, comprising the steps of:
step 1: sending pulverized coal, heated hydrogen and oxygen into a gasification furnace 1 through a nozzle 2.2 of the gasification furnace 1; the granularity of the pulverized coal is 5-90 mu m, the water content is less than 5 percent, and the conveying pressure is 7.8 Mpa; the temperature of the hydrogen is 450 ℃ at the lowest;
step 2: the pulverized coal in the step 1 is mixed with the heated hydrogen and oxygen in a reaction section in the gasification furnace 1, and a hydro-gasification reaction is carried out to generate semicoke and synthesis gas; the semicoke is discharged by the gasification furnace 1 and is cooled and depressurized by a semicoke discharge system 6 to obtain a semicoke product; the reaction temperature in the gasification furnace 1 is 900 ℃ and the reaction pressure is 7.0 Mpa.
And step 3: the pulverized coal in the step 1 and the synthesis gas containing a small amount of semicoke in the step 2 enter a heat energy recovery device 2 for heat exchange, the pulverized coal intercepts the semicoke in the synthesis gas during the heat exchange to obtain a high-temperature mixture, and the high-temperature mixture is deposited at the bottom of the heat energy recovery device 2; the synthesis gas enters a cyclone separator 4 for gas-solid separation, and the separated synthesis gas is directly cooled and separated to obtain a gas product and a liquid oil product; the temperature in the heat recovery device 2 is 850 ℃ and the pressure is 6.9 Mpa.
And 4, step 4: the high-temperature mixture in the step 3 and the solid separated by the cyclone separator 4 are taken as raw materials and are conveyed into the gasification furnace 1 through a pulverized coal pressurizing system 5, and the lowest temperature of the raw materials is 300 ℃; the conveying pressure of the raw material was 7.8 MPa.
In the invention, the pulverized coal exchanges heat with the high-temperature synthesis gas obtained by reaction in the heat energy recovery device 2, and partial volatile matters with stronger activity in the pulverized coal are extracted by pyrolysis under the action of high temperature, so that the content of methane in the synthesis gas is effectively increased; the high-temperature pulverized coal directly reacts with high-temperature hydrogen in the gasification furnace 1 without heating the pulverized coal, so that the reaction time is increased, the carbon conversion rate of the pulverized coal is improved, and the methane content can be improved by about 2% at least according to the conventional gasified hydrogen-coal ratio of 0.3; the temperature of the pulverized coal after heat exchange in the heat energy recovery device 2 is more than or equal to 300 ℃, so that heat energy recovery is realized; high-temperature pulverized coal enters a reaction section in the gasification furnace 1 to participate in hydrogenation reaction, so that the consumption of oxygen and hydrogen is greatly reduced, the energy is saved, and the production cost is reduced.
According to the prior art, the temperature of the pulverized coal entering the gasification furnace 1 is 80 ℃, and the temperature of the pulverized coal returning to the gasification furnace 1 in the invention is 280-300 ℃, so that about 20Nm (Nm) can be saved per ton of coal per hour on average3Hydrogen,/h, and 10Nm3The amount of oxygen per hour. If calculated according to the coal feeding amount of 1000 tons per day, 20000Nm hydrogen can be saved in one day3Oxygen 10000Nm3(ii) a The economic benefit is very considerable.
The foregoing is a preferred embodiment of the present invention, and it will be apparent to those skilled in the art that various modifications and adaptations can be made without departing from the principles of the invention, and such modifications and adaptations are intended to be included within the scope of the invention.
Claims (13)
1. A pulverized coal hydro-gasification system is characterized by comprising a gasification furnace, a heat energy recovery device, a pulverized coal feeding system, a cyclone separator and a pulverized coal pressurizing system;
the gas outlet of the gasification furnace is communicated with the gas inlet of the heat energy recovery device; the discharge hole of the pulverized coal feeding system is communicated with the feed hole of the heat energy recovery device;
the air outlet of the heat energy recovery device is communicated with the air inlet of the cyclone separator; the discharge hole of the heat energy recovery device and the discharge hole of the cyclone separator are both communicated with the feed inlet of the pulverized coal pressurizing system;
and the discharge holes of the pulverized coal pressurizing system and the pulverized coal charging system are communicated with the feed hole of the gasification furnace.
2. The pulverized coal hydrogasification system as claimed in claim 1,
it also includes a semicoke discharge system; and the discharge port of the gasification furnace is communicated with the feed inlet of the semicoke discharging system.
3. The pulverized coal hydrogasification system of claim 1, wherein the pulverized coal charging system comprises a pulverized coal bunker, a pulverized coal atmospheric tank, a pressure swing lock hopper, a pulverized coal charging bucket, a hydrogen source, a nitrogen source, a pulverized coal filter and a flare burner;
the discharge hole of the pulverized coal bunker is communicated with the feed inlet of the pulverized coal normal pressure tank; the discharge hole of the pulverized coal normal pressure tank is communicated with the feed inlet of the pressure-variable lock hopper; the discharge hole of the pressure swing lock hopper is communicated with the feed inlet of the pulverized coal material sending tank; the discharge hole of the pulverized coal material sending tank is respectively communicated with the gasification furnace and the feed hole of the heat energy recovery device;
the hydrogen source and the nitrogen source are both communicated with an air inlet of the pressure swing lock hopper; the air outlet of the variable pressure lock hopper is communicated with the air inlet of the pulverized coal filter; the gas outlet of the pulverized coal filter is communicated with the gas inlet of the torch burner;
a first balance pipe is communicated between the variable pressure lock hopper and the pulverized coal material dispensing tank.
4. The pulverized coal hydrogasification system according to claim 3, wherein a discharge pipe is provided at a discharge port of the pulverized coal bunker, and one end of the discharge pipe is communicated with the discharge port of the pulverized coal bunker; the other end of the discharge pipe is communicated with a feed delivery pipe, and one end of the feed delivery pipe is communicated with the hydrogen source; the other end of the conveying pipe is respectively communicated with the gasification furnace and the feed inlet of the heat energy recovery device.
5. The pulverized coal hydrogasification system of claim 1, wherein the pulverized coal pressurization system comprises a pulverized coal collection tank, a pulverized coal lock hopper, an intermediate distribution tank, a coal gas source, a high temperature filter and a flare burner;
the heat energy recovery device and the discharge hole of the cyclone separator are communicated with the feed inlet of the pulverized coal collecting tank; the discharge hole of the pulverized coal collecting tank is communicated with the feed inlet of the pulverized coal locking hopper, and the discharge hole of the pulverized coal locking hopper is communicated with the feed inlet of the middle material sending tank; the discharge hole of the intermediate material sending tank is communicated with the feed hole of the gasification furnace;
the coal gas source is communicated with the gas inlet of the pulverized coal lock hopper; the gas outlet of the pulverized coal lock hopper is communicated with the gas inlet of the high-temperature filter, and the gas outlet of the high-temperature filter is communicated with the gas inlet of the torch burner;
a second balance pipe is communicated and arranged between the pulverized coal lock hopper and the pulverized coal collecting tank; and a third balance pipe is communicated between the pulverized coal lock hopper and the middle material sending tank.
6. The pulverized coal hydrogasification system of claim 2, wherein the char emission system comprises a char cooler, a char collection tank, a char lock hopper, a char water cooler, a char storage bin, a coal gas source, a nitrogen source, a char filter, and a flare burner;
the discharge hole of the gasification furnace is communicated with the feed inlet of the semicoke cooler; the discharge hole of the semicoke cooler is communicated with the feed inlet of the semicoke collecting tank; the discharge hole of the semicoke collecting tank is communicated with the feed inlet of the semicoke locking hopper; the discharge hole of the semicoke lock hopper is communicated with the feed inlet of the semicoke water cooler; the discharge hole of the semicoke water cooler is communicated with the feed inlet of the semicoke storage bin;
the coal gas source is respectively communicated with the semicoke cooler and the air inlet of the semicoke lock hopper; the nitrogen source is communicated with an air inlet of the semicoke lock hopper;
the air outlet of the semicoke lock hopper is communicated with the air inlet of the semicoke filter; the gas outlet of the semicoke filter is communicated with the gas inlet of the torch burner;
and the semicoke lock hopper is communicated with the semicoke collecting tank through a fourth balance pipe.
7. The pulverized coal hydrogasification system as claimed in claim 1, wherein the heat energy recovery unit comprises a tower body; a plurality of nozzles forming an included angle of 45-90 degrees with the center line of the tower body are uniformly arranged above the inside of the tower body;
the top of the tower body is provided with an air outlet, the side wall of the tower body below the nozzle is provided with an air inlet, and the bottom of the tower body is provided with a discharge hole.
8. The pulverized coal gasification process method using the pulverized coal hydro-gasification system as claimed in any one of claims 1 to 7, characterized by comprising the steps of:
step 1: sending pulverized coal, heated hydrogen and oxygen into a gasification furnace through a gasification furnace nozzle;
step 2: mixing the pulverized coal in the step 1 with the heated hydrogen and oxygen in a reaction section in the gasification furnace, and carrying out hydro-gasification reaction to generate semicoke and synthesis gas;
and step 3: the pulverized coal in the step 1 and the synthesis gas containing a small amount of semicoke in the step 2 enter a heat energy recovery device for heat exchange, the pulverized coal intercepts the semicoke in the synthesis gas during the heat exchange to obtain a high-temperature mixture, and the high-temperature mixture is deposited at the bottom of the heat energy recovery device; the synthetic gas enters a cyclone separator for gas-solid separation, and the separated synthetic gas is directly cooled and separated to obtain a gas product and a liquid oil product;
and 4, step 4: and 3, conveying the high-temperature mixture obtained in the step 3 and the solid separated by the cyclone separator serving as raw materials to a gasification furnace through a pulverized coal pressurizing system.
9. The pulverized coal gasification process according to claim 8, wherein the semicoke in the step 2 is discharged from the gasification furnace and cooled and depressurized by a semicoke discharging system to obtain a semicoke product.
10. The pulverized coal gasification process method according to claim 8, wherein the particle size of the pulverized coal in step 1 is 5-90 μm, and the water content is less than 5%; the temperature of the hydrogen is 450 ℃ at the lowest; the feed temperature in step 4 was a minimum of 300 ℃.
11. The pulverized coal gasification process method as claimed in claim 8, wherein the transportation pressure of the pulverized coal in step 1 and step 2 is 7.6Mpa ± 0.2; the conveying pressure of the raw materials in the step 4 is 7.6Mpa +/-0.2.
12. The pulverized coal gasification process as claimed in claim 8, wherein the reaction temperature in the gasification furnace in step 2 is 700-.
13. The pulverized coal gasification process as claimed in claim 8, wherein the temperature in the heat energy recovery device in step 3 is 750-.
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| JP2012180430A (en) * | 2011-02-28 | 2012-09-20 | Mitsubishi Heavy Ind Ltd | Gasification furnace, gasification combined power generation facility, and method of collecting char of the gasification furnace |
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