CN117603724B - Process for preparing chemical raw material by fractional gas-phase catalytic cracking of oil-rich coal - Google Patents
Process for preparing chemical raw material by fractional gas-phase catalytic cracking of oil-rich coal Download PDFInfo
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- CN117603724B CN117603724B CN202311477875.6A CN202311477875A CN117603724B CN 117603724 B CN117603724 B CN 117603724B CN 202311477875 A CN202311477875 A CN 202311477875A CN 117603724 B CN117603724 B CN 117603724B
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- 239000003245 coal Substances 0.000 title claims abstract description 52
- 238000004523 catalytic cracking Methods 0.000 title claims abstract description 24
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 9
- 239000013064 chemical raw material Substances 0.000 title description 3
- 238000000197 pyrolysis Methods 0.000 claims abstract description 102
- 239000007789 gas Substances 0.000 claims abstract description 57
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 34
- 239000003546 flue gas Substances 0.000 claims abstract description 34
- 239000007787 solid Substances 0.000 claims abstract description 28
- 239000003054 catalyst Substances 0.000 claims abstract description 26
- 238000010438 heat treatment Methods 0.000 claims abstract description 23
- 239000000571 coke Substances 0.000 claims abstract description 17
- 238000005336 cracking Methods 0.000 claims abstract description 17
- 239000002994 raw material Substances 0.000 claims abstract description 16
- 239000000126 substance Substances 0.000 claims abstract description 15
- 238000002156 mixing Methods 0.000 claims abstract description 10
- 239000002918 waste heat Substances 0.000 claims abstract description 10
- 125000005575 polycyclic aromatic hydrocarbon group Chemical group 0.000 claims abstract description 9
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 claims abstract description 7
- 229910052791 calcium Inorganic materials 0.000 claims abstract description 7
- 239000011575 calcium Substances 0.000 claims abstract description 7
- 238000000926 separation method Methods 0.000 claims abstract description 7
- 238000001035 drying Methods 0.000 claims abstract description 5
- 239000008188 pellet Substances 0.000 claims abstract description 4
- 238000007599 discharging Methods 0.000 claims abstract 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 17
- 239000002245 particle Substances 0.000 claims description 11
- 239000002002 slurry Substances 0.000 claims description 11
- 238000011084 recovery Methods 0.000 claims description 5
- 230000000694 effects Effects 0.000 claims description 4
- 238000000465 moulding Methods 0.000 claims description 4
- 238000005728 strengthening Methods 0.000 claims description 4
- YJTKZCDBKVTVBY-UHFFFAOYSA-N 1,3-Diphenylbenzene Chemical group C1=CC=CC=C1C1=CC=CC(C=2C=CC=CC=2)=C1 YJTKZCDBKVTVBY-UHFFFAOYSA-N 0.000 claims description 3
- 239000000853 adhesive Substances 0.000 claims description 3
- 230000001070 adhesive effect Effects 0.000 claims description 3
- 230000002378 acidificating effect Effects 0.000 claims description 2
- 239000002131 composite material Substances 0.000 claims description 2
- 239000002808 molecular sieve Substances 0.000 claims description 2
- 238000004064 recycling Methods 0.000 claims description 2
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 2
- 239000000843 powder Substances 0.000 abstract description 11
- 238000007233 catalytic pyrolysis Methods 0.000 abstract description 9
- 238000002485 combustion reaction Methods 0.000 abstract description 4
- 239000003921 oil Substances 0.000 description 65
- 239000011269 tar Substances 0.000 description 11
- 239000002817 coal dust Substances 0.000 description 5
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- 239000012190 activator Substances 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 239000008187 granular material Substances 0.000 description 3
- 238000000034 method Methods 0.000 description 3
- 230000004913 activation Effects 0.000 description 2
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 239000002283 diesel fuel Substances 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
- 239000003502 gasoline Substances 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N phenol group Chemical group C1(=CC=CC=C1)O ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 description 2
- 230000002269 spontaneous effect Effects 0.000 description 2
- 150000005671 trienes Chemical class 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000007841 coal based oil Substances 0.000 description 1
- 239000011280 coal tar Substances 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- -1 ethylene, propylene Chemical group 0.000 description 1
- 238000005194 fractionation Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 239000003209 petroleum derivative Substances 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 238000012827 research and development Methods 0.000 description 1
- 125000000383 tetramethylene group Chemical group [H]C([H])([*:1])C([H])([H])C([H])([H])C([H])([H])[*:2] 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C4/00—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms
- C07C4/02—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms by cracking a single hydrocarbon or a mixture of individually defined hydrocarbons or a normally gaseous hydrocarbon fraction
- C07C4/06—Catalytic processes
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
- C10G1/002—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal in combination with oil conversion- or refining processes
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/20—C2-C4 olefins
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/30—Aromatics
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Wood Science & Technology (AREA)
- Catalysts (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention provides a process for preparing chemical raw materials by graded gas-phase catalytic pyrolysis of oil-rich coal, which comprises the steps of lifting, drying and gas-solid graded separation of the oil-rich coal smaller than 6mm through a flue gas lifting pipe, discharging flue gas, realizing rapid mixing, heating and rapid pyrolysis of the coal powder and high-temperature circulating semicoke at the top end of a downlink pyrolysis reactor, and separating oil gas and semicoke at the lower part of a riser of the downlink pyrolysis reactor; the pyrolysis oil gas directly enters a downstream catalytic cracking reactor and a high-temperature regenerated cracking catalyst for rapid mixing heating and catalytic cracking, the oil gas at the lower part of a vertical pipe of the downstream catalytic cracking reactor is separated from a spent cracking catalyst, and the pyrolysis oil gas is subjected to a fractionating tower to obtain basic chemical raw materials such as triene triphenyl, 2-4 ring polycyclic aromatic hydrocarbon and the like; the semicoke enters a coke burning lifting pipe for combustion and heating, high-temperature semicoke is separated in a grading way at the top of the lifting pipe, flue gas is guided to the bottom of the flue gas lifting pipe after passing through a waste heat boiler to lift dry rich oil coal, part of semicoke enters the top of a downward pyrolysis reactor for circulation, and part of semicoke is heated by a fluidized bed heat exchanger to produce calcium coke pellets.
Description
Technical Field
The invention provides a process for preparing chemical raw materials by fractional gas phase catalytic pyrolysis of oil-rich coal, belonging to the field of coal chemical industry.
Background
As coal-based oil gas resources integrating coal, oil and gas properties, the oil-rich coal with the oil content of 7% -20% is rich in reserves in China, and the trillion tons of oil gas contained in pyrolysis volatile matters is far higher than the recoverable reserves of the existing petroleum and natural gas in China, so that the oil-rich coal is a potential oil gas resource with low cost and easy obtainment. Pyrolysis upgrading using oil gas as a main product is a clean, efficient and high-value utilization technical route of the rich oil coal, but at present, a single set of megaton demonstration device capable of commercial operation is not available at home and abroad due to the bottlenecks of lower tar yield, higher ash content, coking and blocking of the device, difficult treatment of phenolic wastewater and the like.
In addition, tar produced by pyrolysis and upgrading of the rich oil coal is mainly used for producing gasoline and diesel oil through hydrogenation, the power battery technology is iterated rapidly, the automobile emission standard is stricter, and new energy automobiles show a sudden increase type development trend, so that the consumption of the gasoline and diesel oil is reduced rapidly. The current coal tar utilization technical route taking vehicle fuel as a target is difficult to meet the requirements of a future traffic energy system, and a new technology for directly, cleanly and efficiently preparing basic chemical raw materials and constructing a high-value utilization industrial chain by advanced research and development of the rich coal is needed, so that a guarantee is provided for sustainable high-quality development of the rich coal utilization industry.
Disclosure of Invention
The invention aims to overcome the defects of the existing coal pyrolysis upgrading technology, and provides a process for preparing chemical raw materials by fractional gas-phase catalytic pyrolysis of oil-rich coal, which solves the problems of ash in oil, phenolic wastewater, low tar yield and the like in low-rank coal fluidized bed pyrolysis upgrading, reasonably utilizes waste heat in a comprehensive way, obtains chemical raw materials such as high-added-value triene triphenyl, 2-4 ring polycyclic aromatic hydrocarbon, calcium Jiao Qiutuan/formed coke and the like and fuel gas, and solves the problems of spontaneous combustion of fine coke powder and forming calcium Jiao Qiutuan/type Jiao Reya.
The technical scheme of the invention is as follows:
According to the invention, the rich oil coal and the semicoke are separated in a grading way, and the large and medium particle coal dust and the large and medium particle semicoke are rapidly pyrolyzed by a downlink pyrolysis reactor, so that the problem of ash in oil is solved; the activation of pyrolysis dry gas strengthens the rapid pyrolysis of a coal powder descending bed and the gas-phase catalytic pyrolysis of tar, and solves the problem of low yield of the pyrolysis tar; the fine coal powder lifting pipe is heated by combustion, part of large and medium particle semicoke and fine coke powder are subjected to heat recovery, then cracking oil slurry is bonded and hot-pressed for molding, and the problems of spontaneous combustion of the fine coke powder and molding of calcium Jiao Qiutuan/Jiao Reya are overcome; preparing large amounts of high-value chemical raw materials such as triene triphenyl and 2-4 ring polycyclic aromatic hydrocarbon by directly carrying out gas-phase catalytic pyrolysis on pyrolysis oil gas, and fully utilizing the group composition characteristics of low-temperature fast pyrolysis oil gas in rich oil coal to solve the problem of high-value raw material utilization of pyrolysis oil; after the waste heat is recovered by the waste heat boiler, the high-temperature riser heating/regenerating flue gas is used for drying and lifting the oil-rich coal dust, so that the problems that the oil-rich coal is easy to spontaneously ignite during high-activity drying and high in water content influence the pyrolysis heating rate and the tar yield and the utilization efficiency of the system heat energy are solved.
The invention provides a process for preparing chemical raw materials by graded gas-phase catalytic pyrolysis of oil-rich coal, which is characterized in that oil-rich coal powder smaller than 6mm is heated/regenerated flue gas at 70-300 ℃ through a riser dryer to lift, dry and gas-solid graded separation are carried out, the flue gas is discharged outside, fine coal powder returns to a riser coke burning heater to burn and heat, large and medium particle coal powder flows into the top end of a downlink pyrolysis reactor, is quickly mixed and heated with a 550-1000 ℃ circulating semicoke carrier, and is quickly pyrolyzed at 500-580 ℃ under the strengthening effect of circulating pyrolysis dry gas activated by the circulating semicoke carrier, so as to maximally generate pyrolysis oil gas; separating pyrolysis oil gas from pyrolysis semicoke at the lower part of a downlink pyrolysis reactor, returning the pyrolysis semicoke to a riser coke burning heater for burning and heating at 550-1000 ℃, grading and separating at the top of the riser coke burning heater, recycling high-temperature waste heat from high-temperature heating flue gas through a flue gas heat exchanger, introducing the high-temperature heating flue gas at 70-300 ℃ to the bottom of the riser dryer for lifting dry rich coal, enabling part of large and medium particle pyrolysis semicoke to flow into the top of the downlink pyrolysis reactor as a circulating semicoke carrier, heating fine coke powder and part of large and medium particle pyrolysis semicoke by a coke powder heat exchanger, mixing with atomized pyrolysis slurry oil, and carrying out hot press molding to produce calcium coke pellets/formed coke; directly feeding pyrolysis oil gas at 500-580 ℃ into a downstream catalytic cracking reactor, quickly mixing and heating with a regenerated cracking catalyst at 650-850 ℃, carrying out catalytic cracking at 580-700 ℃, separating the pyrolysis oil gas from a spent cracking catalyst at the lower part of the downstream catalytic cracking reactor, obtaining basic chemical raw materials such as triene triphenyl, 2-4 ring polycyclic aromatic hydrocarbon and the like, pyrolysis slurry oil and pyrolysis dry gas by a fractionating tower, returning the pyrolysis slurry oil as an adhesive of pyrolysis coke powder, and returning part of pyrolysis dry gas as circulating pyrolysis dry gas; the spent cracking catalyst returns to the riser coke-burning regenerator, is burned and regenerated at 650-850 ℃, is subjected to gas-solid separation at the top of the riser coke-burning regenerator, and after the high-temperature regenerated flue gas is subjected to waste heat recovery through the flue gas heat exchanger, the 70-300 ℃ regenerated flue gas is led to the bottom of the riser dryer to lift the dry rich oil coal, and the regenerated cracking catalyst returns to the top of the downstream catalytic cracking reactor to be mixed and reacted with pyrolysis oil gas.
The mixing ratio of the circulating carbocoal carrier and the large and medium particle rich oil coal is 2-10:1, the catalyst-to-oil ratio of pyrolysis oil gas to the catalytic cracking catalyst is 4-10.
The catalytic cracking catalyst is an acidic molecular sieve catalyst, an alkaline porous catalyst or an acid-base composite catalyst.
The coke powder heat exchanger is a solid moving bed heat collector or a fluidized gas-solid external heat collector.
The present invention will be described in detail with reference to examples.
Drawings
FIG. 1 is a schematic process diagram of the present invention. The drawings of the drawings are as follows:
1. The device comprises a rich oil coal charging port 2, a flue gas heat exchanger 3, a draught fan 4, a riser dryer 5, a coal dust primary gas-solid separator 6, a coal dust secondary gas-solid separator 7, a heating flue gas outlet 8, a downlink pyrolysis reactor 9, a pyrolysis dry gas activator 10, a semicoke distribution return device 11, a pyrolysis oil gas-solid separator 12, a coke powder return device 13, a riser coke-burning heater 14, a semicoke primary gas-solid separator 15, a semicoke secondary gas-solid separator 16, a hot press forming machine 17, a downlink catalytic pyrolysis reactor 18, a pyrolysis oil gas-solid separator 19, a spent pyrolysis catalyst return device 20, a riser coke regenerator 21, a regenerated flue gas-solid separator 22, a pyrolysis dry gas outlet 23, a triene outlet 24, a triphenyl outlet 25, a 2-4 ring condensed ring aromatic hydrocarbon outlet a, fine coke powder b, pyrolysis oil slurry c and a cyclic pyrolysis dry gas.
The process features of the present invention are described in detail below with reference to the accompanying drawings and examples.
Detailed Description
In the embodiment, a large amount of oil-rich coal smaller than 6mm enters a riser dryer 4 through an oil-rich coal charging port 1, is heated/regenerated flue gas at 70-300 ℃ after being recycled by a flue gas heat exchanger 2 and pressurized by a draught fan 3 for lifting and drying, and is subjected to gas-solid fractionation at the top of the riser dryer 4; the large and medium particle coal powder obtained by the separation of the coal powder primary gas-solid separator 5 flows into the top end of the downward pyrolysis reactor 8, is quickly mixed with the circulating carbocoal carrier at 550-1000 ℃ and heated, and is quickly pyrolyzed at 500-580 ℃ under the strengthening effect of hydrogen and small molecular hydrocarbon free radicals generated by the activation of the circulating carbocoal carrier by the circulating pyrolysis dry gas through the pyrolysis dry gas activator 9, so as to generate pyrolysis oil gas to the maximum extent; Fine coal powder separated by the coal powder secondary gas-solid separator 6 is returned to the riser tube burning heater 13 for burning and heating, and flue gas is discharged through the flue gas outlet 7; pyrolysis oil gas and pyrolysis semicoke are separated from each other through a pyrolysis oil gas-solid separator 11 at the lower part of the downlink pyrolysis reactor 8, and the pyrolysis semicoke is returned to a riser coke burning heater 13 through a coke powder returning device 12 together with fine coal powder a for burning and heating at 550-1000 ℃, and is graded and separated at the top of the riser coke burning heater 13; part of large and medium granule pyrolysis semicoke obtained by separating the semicoke primary gas-solid separator 14 flows into the top of the downstream pyrolysis reactor 8 through the semicoke distribution material returning device 10 as a circulating semicoke carrier, part of large and medium granule pyrolysis semicoke flows into the pyrolysis dry gas activator 9 to activate the circulating pyrolysis dry gas for strengthening the quick pyrolysis reaction of pulverized coal to increase the oil quality, and part of large and medium granule pyrolysis semicoke and fine coke powder obtained through the semicoke secondary gas-solid separator 15 are mixed with atomized pyrolysis slurry b after being heated by a coke powder heat exchanger and subjected to hot press forming by the hot press forming machine 16 to produce calcium coke pellets/formed coke; after the heating flue gas separated by the semicoke secondary gas-solid separator 15 is subjected to high-temperature waste heat recovery through a flue gas heat exchanger, the heating flue gas at 70-300 ℃ is guided to the bottom of the riser dryer 4 to lift and dry the rich oil coal; Pyrolysis oil gas at 500-580 ℃ directly enters a downstream catalytic cracking reactor 17 and a regenerated cracking catalyst at 650-850 ℃ obtained by separating the pyrolysis oil gas and the solid separator of regenerated flue gas, the temperature is raised by rapid mixing, catalytic cracking is carried out at 580-700 ℃, the pyrolysis oil gas and the spent cracking catalyst are separated through a pyrolysis oil gas and solid separator 18 at the lower part of the downstream catalytic cracking reactor 17, the pyrolysis oil gas is subjected to a fractionating tower to obtain triene triphenyl from a triene outlet 23 and a triphenyl outlet 24, basic chemical raw materials such as 2-4 ring polycyclic aromatic hydrocarbon are obtained from a 2-4 ring polycyclic aromatic hydrocarbon outlet 25, pyrolysis oil slurry b is obtained at the bottom of the tower, and a pyrolysis dry gas part at the top of the tower is discharged from a pyrolysis dry gas outlet 22, Returning part of the pyrolysis dry gas as circulating pyrolysis dry gas a, and returning pyrolysis slurry oil b to the hot briquetting machine 16 as an adhesive of pyrolysis coke powder; The to-be-regenerated cracking catalyst separated from the cracking oil gas-solid separator 18 returns to the riser burnt regenerator 20 through the to-be-regenerated cracking catalyst returning device 19, is burnt and regenerated at 650-850 ℃, is subjected to gas-solid separation at the top of the riser burnt regenerator 20, and after the high-temperature regenerated flue gas is subjected to waste heat recovery through the flue gas heat exchanger 2, the 70-300 ℃ regenerated flue gas is pressurized by the induced draft fan 3 and is led to the bottom of the riser dryer 4 to lift dry rich oil coal, and the regenerated cracking catalyst separated through the regenerated flue gas-solid separator returns to the top of the downstream catalytic cracking reactor 17 to be mixed and reacted with pyrolysis oil gas.
According to the process for preparing chemical raw materials by fractional gas-phase catalytic pyrolysis of the oil-rich coal, provided by the invention, the processes of preparing the triene triphenyl and the 2-4 ring polycyclic aromatic hydrocarbon by carrying out rapid pyrolysis on the oil-rich coal activated and intensified by pyrolysis dry gas and carrying out direct gas-phase catalytic pyrolysis on pyrolysis oil gas are coupled, the dry coal dust and the semicoke are separated in a fractional manner and utilized in a classified manner, the oil with ash is eliminated from the source, the relative yield of tar is more than 130% of the theoretical tar yield, the impurity content in the oil is less than 0.1%, and the oil is converted to produce the triene triphenyl and the 2-4 ring polycyclic aromatic hydrocarbon chemical raw materials in a maximized manner. The chemical raw material is prepared by using the eastern rich oil coal with the oil content of 13.4 percent as the raw material through fractional gas phase catalytic cracking, and the relative yield of tar is improved to 140 percent; the total yield of ethylene, propylene and butylene is 19.5%, the alkene-alkane ratio is 15, the crude benzene is 15%, the bi-to tetracyclic aromatic hydrocarbon fraction is 50.5%, the tar deoxidation rate is 45%, the desulfurization rate is 60% and the denitrification rate is 40% based on tar.
Claims (2)
1. The process for preparing chemical raw materials by fractional gas phase catalytic cracking of the oil-rich coal is characterized by comprising the following steps of: heating the oil-rich pulverized coal smaller than 6mm by using 70-300 ℃ to regenerate flue gas, lifting and drying by a riser dryer, carrying out gas-solid classification separation, discharging the flue gas outwards, returning fine pulverized coal to a riser burning heater for burning and heating, enabling large and medium-sized pulverized coal to flow into the top end of a downlink pyrolysis reactor, quickly mixing and heating with a 550-1000 ℃ circulating semicoke carrier, quickly pyrolyzing at 500-580 ℃ under the strengthening effect of circulating pyrolysis dry gas activated by the circulating semicoke carrier, and maximally generating pyrolysis oil gas; the mixing ratio of the circulating carbocoal carrier and the large and medium particle rich oil coal is 2-10:1, the catalyst-to-oil ratio of the catalytic cracking catalyst to pyrolysis oil gas is 4-10:1, a step of; separating pyrolysis oil gas from pyrolysis semicoke at the lower part of a downlink pyrolysis reactor, returning the pyrolysis semicoke to a riser coke burning heater for burning and heating at 550-1000 ℃, grading and separating at the top of the riser coke burning heater, recycling high-temperature waste heat from high-temperature heating flue gas through a flue gas heat exchanger, introducing the high-temperature heating flue gas at 70-300 ℃ to the bottom of the riser dryer to lift dry rich coal, enabling part of large and medium particle pyrolysis semicoke to flow into the top of the downlink pyrolysis reactor as a circulating semicoke carrier, heating fine coke powder and part of large and medium particle pyrolysis semicoke by a coke powder heat exchanger, mixing with atomized pyrolysis slurry oil, and carrying out hot press molding to produce calcium coke pellets or formed coke; the catalytic cracking catalyst is an acidic molecular sieve catalyst, an alkaline porous catalyst or an acid-base composite catalyst; directly feeding pyrolysis oil gas at 500-580 ℃ into a downstream catalytic cracking reactor, quickly mixing and heating with a regenerated cracking catalyst at 650-850 ℃, carrying out catalytic cracking at 580-700 ℃, separating the pyrolysis oil gas from a spent cracking catalyst at the lower part of the downstream catalytic cracking reactor, obtaining trienyl triphenyl, 2-4 ring polycyclic aromatic hydrocarbon, pyrolysis slurry oil and pyrolysis dry gas by a fractionating tower, returning the pyrolysis slurry oil as an adhesive of pyrolysis coke powder, and returning part of pyrolysis dry gas as circulating pyrolysis dry gas; the spent cracking catalyst returns to the riser coke-burning regenerator, is burned and regenerated at 650-850 ℃, is subjected to gas-solid separation at the top of the riser coke-burning regenerator, and after the high-temperature regenerated flue gas is subjected to waste heat recovery through the flue gas heat exchanger, the 70-300 ℃ regenerated flue gas is led to the bottom of the riser dryer to lift the dry rich oil coal, and the regenerated cracking catalyst returns to the top of the downstream catalytic cracking reactor to be mixed and reacted with pyrolysis oil gas.
2. The process for preparing chemical raw materials by fractional gas phase catalytic cracking of oil-rich coal according to claim 1, which is characterized in that: the coke powder heat exchanger is a solid moving bed heat collector or a fluidized gas-solid external heat collector.
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| CN101186838A (en) * | 2006-11-20 | 2008-05-28 | 克里斯蒂安·科赫 | High-power tank mixer for catalytic oil suspensions |
| CA2738011A1 (en) * | 2010-04-28 | 2011-10-28 | Galtenco Technology, Ltd. | Process for separating bitumen from other constituents in mined, bitumen rich ore |
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| CA2738011A1 (en) * | 2010-04-28 | 2011-10-28 | Galtenco Technology, Ltd. | Process for separating bitumen from other constituents in mined, bitumen rich ore |
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