CN109280561A - A kind of method of naphtha or the low-temperature catalyzed reaction propylene co-production aromatic hydrocarbons processed of lighter hydrocarbons - Google Patents
A kind of method of naphtha or the low-temperature catalyzed reaction propylene co-production aromatic hydrocarbons processed of lighter hydrocarbons Download PDFInfo
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- CN109280561A CN109280561A CN201811440380.5A CN201811440380A CN109280561A CN 109280561 A CN109280561 A CN 109280561A CN 201811440380 A CN201811440380 A CN 201811440380A CN 109280561 A CN109280561 A CN 109280561A
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- naphtha
- reaction
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- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 75
- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 73
- 238000000034 method Methods 0.000 title claims abstract description 64
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 title claims abstract description 52
- 150000004945 aromatic hydrocarbons Chemical class 0.000 title claims abstract description 39
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 title claims abstract description 32
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 13
- 238000006555 catalytic reaction Methods 0.000 title claims abstract description 12
- 239000004215 Carbon black (E152) Substances 0.000 claims abstract description 50
- 238000006243 chemical reaction Methods 0.000 claims abstract description 50
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 42
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 38
- 239000002994 raw material Substances 0.000 claims abstract description 38
- 239000003054 catalyst Substances 0.000 claims abstract description 28
- 239000000047 product Substances 0.000 claims abstract description 24
- 238000000926 separation method Methods 0.000 claims abstract description 11
- 238000004523 catalytic cracking Methods 0.000 claims abstract description 10
- 230000009471 action Effects 0.000 claims abstract description 8
- 238000009826 distribution Methods 0.000 claims abstract description 8
- -1 ethylene, propylene Chemical group 0.000 claims abstract description 8
- 239000007795 chemical reaction product Substances 0.000 claims abstract description 4
- 238000004064 recycling Methods 0.000 claims abstract description 3
- 239000000203 mixture Substances 0.000 claims description 19
- 150000001336 alkenes Chemical class 0.000 claims description 18
- 238000005336 cracking Methods 0.000 claims description 15
- 238000005899 aromatization reaction Methods 0.000 claims description 12
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 9
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 claims description 8
- 239000000463 material Substances 0.000 claims description 7
- 150000001335 aliphatic alkanes Chemical class 0.000 claims description 6
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 claims description 5
- 238000006356 dehydrogenation reaction Methods 0.000 claims description 5
- 238000005265 energy consumption Methods 0.000 claims description 5
- 239000005977 Ethylene Substances 0.000 claims description 4
- 210000004556 brain Anatomy 0.000 claims description 3
- 238000006384 oligomerization reaction Methods 0.000 claims description 3
- 239000004575 stone Substances 0.000 claims description 3
- 238000004939 coking Methods 0.000 claims description 2
- 230000009849 deactivation Effects 0.000 claims description 2
- 238000002156 mixing Methods 0.000 claims description 2
- 230000008569 process Effects 0.000 abstract description 13
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 abstract description 12
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical compound CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 abstract description 5
- 238000004230 steam cracking Methods 0.000 abstract description 5
- 239000006227 byproduct Substances 0.000 abstract description 4
- 230000008901 benefit Effects 0.000 abstract description 3
- 238000010438 heat treatment Methods 0.000 abstract description 3
- 239000007789 gas Substances 0.000 description 19
- 238000005516 engineering process Methods 0.000 description 12
- 239000007788 liquid Substances 0.000 description 12
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 9
- 238000001833 catalytic reforming Methods 0.000 description 7
- 229910052751 metal Inorganic materials 0.000 description 7
- 239000002184 metal Substances 0.000 description 7
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical class [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 7
- 239000002808 molecular sieve Substances 0.000 description 6
- PNEYBMLMFCGWSK-UHFFFAOYSA-N Alumina Chemical compound [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 5
- VQTUBCCKSQIDNK-UHFFFAOYSA-N Isobutene Chemical compound CC(C)=C VQTUBCCKSQIDNK-UHFFFAOYSA-N 0.000 description 4
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 4
- 125000003118 aryl group Chemical group 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 238000005984 hydrogenation reaction Methods 0.000 description 4
- NNPPMTNAJDCUHE-UHFFFAOYSA-N isobutane Chemical compound CC(C)C NNPPMTNAJDCUHE-UHFFFAOYSA-N 0.000 description 4
- 238000006317 isomerization reaction Methods 0.000 description 4
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 3
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 238000010521 absorption reaction Methods 0.000 description 3
- 238000009835 boiling Methods 0.000 description 3
- 238000007233 catalytic pyrolysis Methods 0.000 description 3
- 238000010168 coupling process Methods 0.000 description 3
- 238000001125 extrusion Methods 0.000 description 3
- 239000001257 hydrogen Substances 0.000 description 3
- 229910052739 hydrogen Inorganic materials 0.000 description 3
- 238000002352 steam pyrolysis Methods 0.000 description 3
- VXNZUUAINFGPBY-UHFFFAOYSA-N 1-Butene Chemical compound CCC=C VXNZUUAINFGPBY-UHFFFAOYSA-N 0.000 description 2
- HIXDQWDOVZUNNA-UHFFFAOYSA-N 2-(3,4-dimethoxyphenyl)-5-hydroxy-7-methoxychromen-4-one Chemical compound C=1C(OC)=CC(O)=C(C(C=2)=O)C=1OC=2C1=CC=C(OC)C(OC)=C1 HIXDQWDOVZUNNA-UHFFFAOYSA-N 0.000 description 2
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- 241000196324 Embryophyta Species 0.000 description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 2
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 2
- 238000004458 analytical method Methods 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 229910002091 carbon monoxide Inorganic materials 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 239000000571 coke Substances 0.000 description 2
- 150000001875 compounds Chemical class 0.000 description 2
- 230000008878 coupling Effects 0.000 description 2
- 238000005859 coupling reaction Methods 0.000 description 2
- 150000001924 cycloalkanes Chemical class 0.000 description 2
- 230000002950 deficient Effects 0.000 description 2
- 238000007323 disproportionation reaction Methods 0.000 description 2
- RTZKZFJDLAIYFH-UHFFFAOYSA-N ether Substances CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 description 2
- 238000000605 extraction Methods 0.000 description 2
- 239000001282 iso-butane Substances 0.000 description 2
- 235000013847 iso-butane Nutrition 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 239000001294 propane Substances 0.000 description 2
- 238000007670 refining Methods 0.000 description 2
- IJDNQMDRQITEOD-UHFFFAOYSA-N sec-butylidene Natural products CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 2
- 238000000638 solvent extraction Methods 0.000 description 2
- 239000003381 stabilizer Substances 0.000 description 2
- 238000003786 synthesis reaction Methods 0.000 description 2
- 238000012360 testing method Methods 0.000 description 2
- 229910052684 Cerium Inorganic materials 0.000 description 1
- 241001269238 Data Species 0.000 description 1
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 1
- 241000282326 Felis catus Species 0.000 description 1
- 229910002651 NO3 Inorganic materials 0.000 description 1
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 description 1
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 1
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 description 1
- 244000275012 Sesbania cannabina Species 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 125000002009 alkene group Chemical group 0.000 description 1
- WNROFYMDJYEPJX-UHFFFAOYSA-K aluminium hydroxide Chemical compound [OH-].[OH-].[OH-].[Al+3] WNROFYMDJYEPJX-UHFFFAOYSA-K 0.000 description 1
- 229910021502 aluminium hydroxide Inorganic materials 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 229910052787 antimony Inorganic materials 0.000 description 1
- 150000001491 aromatic compounds Chemical class 0.000 description 1
- 229910052785 arsenic Inorganic materials 0.000 description 1
- 239000011230 binding agent Substances 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000004587 chromatography analysis Methods 0.000 description 1
- 239000000084 colloidal system Substances 0.000 description 1
- 238000005094 computer simulation Methods 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 238000005520 cutting process Methods 0.000 description 1
- 238000003795 desorption Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 150000001993 dienes Chemical class 0.000 description 1
- 238000007598 dipping method Methods 0.000 description 1
- 238000006266 etherification reaction Methods 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 238000011065 in-situ storage Methods 0.000 description 1
- 238000001802 infusion Methods 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- JEIPFZHSYJVQDO-UHFFFAOYSA-N iron(III) oxide Inorganic materials O=[Fe]O[Fe]=O JEIPFZHSYJVQDO-UHFFFAOYSA-N 0.000 description 1
- 235000015110 jellies Nutrition 0.000 description 1
- 239000008274 jelly Substances 0.000 description 1
- 229910052746 lanthanum Inorganic materials 0.000 description 1
- MRELNEQAGSRDBK-UHFFFAOYSA-N lanthanum oxide Inorganic materials [O-2].[O-2].[O-2].[La+3].[La+3] MRELNEQAGSRDBK-UHFFFAOYSA-N 0.000 description 1
- 230000001404 mediated effect Effects 0.000 description 1
- 229910044991 metal oxide Inorganic materials 0.000 description 1
- 150000004706 metal oxides Chemical class 0.000 description 1
- 238000000465 moulding Methods 0.000 description 1
- 229910052759 nickel Inorganic materials 0.000 description 1
- 229910017604 nitric acid Inorganic materials 0.000 description 1
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- KTUFCUMIWABKDW-UHFFFAOYSA-N oxo(oxolanthaniooxy)lanthanum Chemical compound O=[La]O[La]=O KTUFCUMIWABKDW-UHFFFAOYSA-N 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 229910052698 phosphorus Inorganic materials 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 229910052761 rare earth metal Inorganic materials 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 238000005070 sampling Methods 0.000 description 1
- 239000000377 silicon dioxide Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 238000010025 steaming Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 238000004227 thermal cracking Methods 0.000 description 1
- 238000005303 weighing Methods 0.000 description 1
- 239000008096 xylene Substances 0.000 description 1
- 229910052725 zinc Inorganic materials 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
- C10G55/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process
- C10G55/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only
- C10G55/06—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only including at least one catalytic cracking step
-
- 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
- C10G61/00—Treatment of naphtha by at least one reforming process and at least one process of refining in the absence of hydrogen
- C10G61/02—Treatment of naphtha by at least one reforming process and at least one process of refining in the absence of hydrogen 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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1037—Hydrocarbon 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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1037—Hydrocarbon fractions
- C10G2300/1044—Heavy gasoline or naphtha having a boiling range of about 100 - 180 °C
-
- 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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/4006—Temperature
-
- 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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/4012—Pressure
-
- 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
-
- 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
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
Abstract
It is a kind of using naphtha or lighter hydrocarbons as the process of the low-temperature catalyzed reaction propylene co-production aromatic hydrocarbons processed of raw material.This method step includes: that raw material naphtha or lighter hydrocarbons enter fixed bed reactors after heat exchanger exchanges heat and/or heats stove heating, low-temperature catalyzed reaction is carried out under the action of special catalyst, reaction product obtains the aromatic hydrocarbons such as ethylene, propylene, the toluene of four light dydrocarbon hydrocarbon of carbon and by-product and dimethylbenzene after separation system, and four light dydrocarbon hydrocarbon of a portion carbon is recycled back into reactor.This process carries out in fixed bed reactors, and catalytic reaction temperature is lower than traditional naphtha catalytic cracking technique, well below traditional naphtha steam cracking technique；By the way of the recycling of self-produced four light dydrocarbon hydrocarbon of carbon, reaction heat is taken full advantage of；The product distribution of this method is adjustable, and can obtain higher propylene and aromatics yield simultaneously.
Description
Technical field
The present invention relates to a kind of using naphtha or lighter hydrocarbons as the technique of the low-temperature catalyzed reaction propylene co-production aromatic hydrocarbons processed of raw material
Method.Specifically one kind is in fixed bed reactors, under the action of lower reaction temperature and feature catalyst, stone brain
Oil or lighter hydrocarbons cracking reaction generate the propylene product of high yield, the method for co-production aromatic hydrocarbons.
Background technique
Propylene is one of most basic most important raw material in modern petrochemical field.In recent years, inner propene in the world
Demand just increase very fast, and petroleum resources non-renewable at the same time are increasingly deficient.About 60% propylene all comes at present
Derived from traditional naphtha steam pyrolysis technology, but not only reaction temperature is high for traditional naphtha steam pyrolysis technology,
Energy consumption is high, and productivity of propylene is low.In order to which imbalance between supply and demand and the naphtha resource of alleviating the propylene to become increasingly conspicuous are increasingly deficient
With the contradiction of steam thermal cracking low yield, naphtha catalytic cracking technology is come into being.
Compared with traditional steam pyrolysis technology, naphtha catalytic cracking technology is by reaction temperature from 800~1000 DEG C
50~200 DEG C are reduced, propene yield is also increased to 15%~38% from about 10%.The application of the technology not only avoids steam and splits
The damage of high temperature energy consumption and hot conditions to equipment etc. is solved, and takes full advantage of naphtha resource, with stone brain as much
Oil can produce more propylene products.Deep catalytic cracking technology was just more and more weighed by various countries researcher over the past two years
Depending on.
As propylene, aromatic hydrocarbons is also important basic organic synthesis raw material, especially triphen (i.e. benzene, toluene and diformazan
Benzene, i.e. BTX).The most important production ways of aromatic hydrocarbons are naphtha catalytic reformings at present, obtain aromatic hydrocarbons mixture, are adsorbed, is cold
The processes by-product such as jelly, rectifying obtains the aromatic hydrocarbon product to conform to quality requirements using process combinations such as isomerization, disproportionations.
Currently, there are many research that naphtha catalytic cracking prepares ethylene, propylene, but can coproduction high yield aromatic hydrocarbons is very simultaneously
It is few.It is existing can simultaneously coproduction high yield aromatic hydrocarbons technique also only and catalytic reforming aromatic hydrocarbons group technology or use
The coupling technique technology of two kinds or more raw materials.
CN104927915A discloses a kind of " using naphtha as the method for olefin production and aromatic hydrocarbons ".This method passes through
Naphtha liquid liquid is extracted to obtain extraction oil and be raffinated oil, and will be carried out steam cracking containing alkane and raffinating oil for cycloalkane, is obtained
Drippolene obtains the extraction oil containing aromatic hydrocarbons and cycloalkane that hydrofined gasoline and liquid liquid extract after hydrofinishing
Catalytic reforming is carried out together, produces light olefin and aromatic hydrocarbons.According to described in embodiment, BTX yield 35.7%, total aromatic hydrocarbons (contains
C8C9 aromatic hydrocarbons) yield 45.4%, yield of ethene 22.5%, propene yield 11.6%.The technique propene yield is low, and process is complicated,
It is related to the extracting of liquid liquid, hydrofinishing, steam cracking, catalytic reforming etc..
CN101759513A discloses " a kind of utilization method of naphtha ".This method adsorption separation method divides naphtha
From at the component containing n-alkane and containing the component of non-n-alkane, wherein n-alkane is cut into C5C6 fraction and >=C7 evaporates
Point, C5C6 fraction obtains C5C6 isoparaffin after isomerization, and >=C7 fraction carries out catalytic pyrolysis and obtains ethylene, propylene, non-positive structure
Alkane component carries out catalytic reforming and obtains aromatic hydrocarbons.By embodiment as it can be seen that this method aromatics yield is up to 59.2%, ethylene and propylene
Total recovery can reach 20.8%.The technique propene yield is not high, and process is complicated, is related to rectifying cutting fraction, isomerization, catalysis
Reform etc..
CN1721510A discloses " a kind of method and apparatus for producing low-carbon alkene and aromatic hydrocarbons ".This method is by raw material low-carbon
Catalytic pyrolysis is carried out after hydrogenation of olefins processing, obtained naphtha obtains aromatic hydrocarbons and pumping after carrying out selective hydrogenation, solvent extraction
Excess oil, devaporation cracker of raffinating oil obtain the low-carbon alkenes such as ethylene, propylene.Wherein catalytic cracking reaction device is moving bed, stream
Change bed etc..This method propene yield can reach 30%, can aromatic hydrocarbons of the coproduction rich in toluene and dimethylbenzene.The process unit includes adding
Hydrogen processing unit, cat-cracker, steam cracking device, selective hydrogenation device, solvent extraction apparatus etc..
CN102803184A discloses " production of light olefin and aromatic compounds ".This method is by the original comprising alkane
Expect that first dehydrogenation obtains the logistics of olefin-containing, then olefin-containing logistics is introduced into cracking of olefins area, reaction generates ethylene, propylene, aromatic hydrocarbons
With heavy hydrocarbon by-product, by the alkadienes of C5~C11 range in heavy hydrocarbon by-product, chosen property is split after adding hydrogen into alkene
Change area.This method does not have specific embodiment, and only under the premise of no catalytic reforming, this method can reach third for computer simulation
Alkene yield 50.38%, triphen yield 16%.The technique includes at least dehydrogenation unit, olefin cracking device, selective hydrogenation device
Deng.
CN108017496A discloses a kind of " devices and methods therefor of production alkene and aromatic hydrocarbons ".There are two types of former for this method
Material, respectively light hydrocarbon feedstocks and oxygen-containing compound material.Both raw materials separately react in two kinds of reactors.Light hydrocarbon feedstocks exist
Reaction obtains the product rich in ethylene, propylene in riser reactor, and oxygen-containing compound material produces richness in a fluidized bed reactor
Product containing aromatic hydrocarbons.This method propene yield is no more than 13.6%, aromatics yield 28.2%.
Summary of the invention
The object of the present invention is to provide one kind using naphtha or lighter hydrocarbons as the low-temperature catalyzed reaction of raw material propylene co-production virtue processed
The process of hydrocarbon.This method makes full use of reaction heat effect, substantially reduces plant energy consumption, and can obtain simultaneously high attached in high yield
Value added propylene and aromatic hydrocarbon product improves oil refining enterprise's economic benefit.
To achieve the above object, the present invention the following steps are included:
(1) gas mixture heat exchange after what raw material naphtha or lighter hydrocarbons and reactor bottom flowed out react and/or directly
Heating reaches preheating temperature；
(2) after naphtha or lighter hydrocarbons are mixed with self-produced four light dydrocarbon hydrocarbon of carbon, enter from reactor head；
(3) the alkene group under the action of feature catalyst loaded in fixed bed reactors, in self-produced four light dydrocarbon hydrocarbon of carbon
The raw overlapping of distribution, cyclisation, aromatization generate macromolecular hydrocarbon, simultaneously because exothermic heat of reaction increases oil gas temperature；Naphtha
Or lighter hydrocarbons absorb a large amount of heat, and the reaction such as dehydrogenation, cracking, overlapping, cyclisation and aromatisation occurs, generates and contains target product propylene
With the hydrocarbon mixture of aromatic hydrocarbons；
(4) hydrocarbon mixture is flowed out from reactor bottom, into subsequent separation system, the ethylene of recycling reaction generation, third
Alkene and aromatic hydrocarbons, the four light dydrocarbon hydrocarbon of part carbon for reacting generation is recycled to step (2), into reactor together with raw material.
Raw material naphtha of the present invention is straight-run naphtha, cat cracked naphtha, field condensate, is hydrocracked
One of naphtha is a variety of.
The raw material lighter hydrocarbons refer to the alkane of four~carbon of carbon ten and cycloalkane hydrocarbon mixture as main component.
Reactor of the present invention is fixed bed reactors, is also possible to fluidized-bed reactor.
Raw material naphtha or lighter hydrocarbons under the action of lower reaction temperature and feature catalyst, occur cracking reaction rather than
Cracking reaction, it is still necessary to absorb a large amount of heat.A part of self-produced four light dydrocarbon hydrocarbon of carbon is recycled back to reactor by the present invention, in catalyst
Under the action of alkene oligomerization occurs, cyclisation, aromatization generate macromolecular hydrocarbon, while a large amount of reaction heat can be released, this portion
Reaction thermal energy is divided to provide heat for the cracking reaction of naphtha, energy consumption needed for greatly reducing entire technique.
Two reactions, the i.e. aromatization of the cracking reaction of naphtha and recycled olefins, carry out in a reactor.
Aromatization provides heat for cracking reaction, while this partial heat is cracked into reactive absorption, in turn avoids aromatisation
React bring temperature runaway etc..
Self-produced four light dydrocarbon hydrocarbon of carbon is recycled back to reactor in the present invention, can not only make full use of reaction heat, and can mention significantly
The yield of high target product propylene and aromatic hydrocarbons.
The present invention can control reaction temperature by adjusting the internal circulating load of self-produced four light dydrocarbon hydrocarbon of carbon, and regulation reaction produces
Object distribution, obtains ideal target product yield.When internal circulating load increases, aromatics yield be will increase, and propene yield is affected；
When internal circulating load is reduced, propene yield be will increase, and aromatics yield is affected.Suitable self-produced four light dydrocarbon hydrocarbon internal circulating load of carbon is
0.01~0.5 times of raw material feed rate.
In the present invention, in order to meet the required heat of raw material cracking, methanol and/or other can also be added in the feed to be had
Machine oxygenatedchemicals, or coupled using other technologies route with the reaction process with exothermic effect.
In the present invention, in order to reduce the coking and deactivation of catalyst, suitable quantity of water steaming can be added in raw material naphtha or lighter hydrocarbons
The weight ratio of gas, suitable water and naphtha is 0.01~0.5.
In step (1), raw material naphtha or lighter hydrocarbons with react after gas mixture heat exchange and/or directly heat and reach pre-
Hot temperature.
In step (2), after naphtha or lighter hydrocarbons are mixed with self-produced four light dydrocarbon hydrocarbon of carbon, enter from reactor head.
In step (3), catalytic reaction condition in reactor are as follows: 460~540 DEG C of reaction temperature, reaction pressure 0.1~
0.25MPa, 0.2~1.5h of weight (hourly) space velocity (WHSV)-1。
In step (4), the gas mixture for reacting generation is flowed out from reactor bottom, is dropped through heat exchanger heat exchange, water cooler
Enter separation system after temperature.Separation system is method well-known to those skilled in the art, including absorbing-stabilizing system and rectifying
System.The four light dydrocarbon hydrocarbon of target product propylene, aromatic hydrocarbons and carbon of this method can be obtained through separation system, a part of four light dydrocarbon hydrocarbon of carbon draws
Device goes to gas subsystem or tank field out, and the self-produced four light dydrocarbon hydrocarbon of carbon of another part is recycled back to reactor, directly urges from reactor
Enter between agent bed, or just mixed before entering the reactor with raw material, enters reactor together.
In industrial implementation, the gas mixture of reactor bottom outflow is exchanged heat and enters absorption and desorption system after liquid separation tank
System, separates dry gas and heavier component.Dry gas emptying or freshening.The material one of this part heavier component and the outflow of liquid separation pot bottom
It rises and enters stabilizer, separate liquefied gas and aromatic naphtha containing propylene, the liquefied gas containing propylene further divides by depropanizing tower etc.
Propane, propylene and C4, C5 hydrocarbon out.C4 hydrocarbon is divided into two strands, one is drawn directly as product liquefied gas, one Returning reactor returns
Refining.C5 hydrocarbon is also classified into two parts, most of Returning reactor freshening, and fraction is drawn directly as product.Go out from stabilizer bottom
The aromatic naphtha come goes to aromatics seperation system, obtains aromatic hydrocarbon product through isomerization, disproportionation etc..
Feature catalyst used in the present invention is metal-modified molecular sieve catalyst, and catalyst includes 0.1~10%
Modified metal-oxide, 40~90% molecular sieves, 10~50% aluminium oxide.The preferred HZSM-5, HZSM-11 of molecular sieve used,
One of modenite, USY molecular sieve, two or more, more preferably HZSM-5, modenite or both it is mixed
Close object.Collectively as the carrier of metal, metal loaded on catalyst using infusion process for molecular sieve and alumina binder.
The modified metal of load includes (1) VIII group or Group IIB element, preferably one of Fe, Co, Ni, Zn, Ga, Cd
Or a variety of, (2) VA race element, preferably one of P, As, Sb or a variety of, (3) rare earth element, preferably one of La, Ce or
Two kinds.
The present invention can obtain suitable distribution of reaction products, obtain by adjusting the content of modified metal in catalyst
Ideal target product yield.
The forming method of catalyst is road known to those skilled in the art in the present invention, such as extrusion, tabletting, round as a ball, drop
Ball.The solids such as molecular sieve, aluminium hydroxide, sesbania powder are uniformly mixed, suitable quantity of water and acid (hydrochloric acid, nitric acid or acetic acid) is added, are squeezed
Pressure is mediated, and the dry fracture of last extrusion is in strip or extrusion is round as a ball at spherical shape；Or all raw materials are mixed and made into colloid, in heat
Drop ball is at spherical shape in oil or oily ammonia bath.Catalyst after molding is dry under conditions of room temperature~150 DEG C, can with metal after dry
The method of soluble (usually nitrate) dipping by metal deposit to catalyst, then 400~600 DEG C at a temperature of,
1~12h is roasted in air or vapor atmosphere to get catalyst of the invention is arrived.
The present invention has the effect that
(1) compared with traditional preparing propylene by catalytic cracking technology, the present invention is reacted using fixed bed reactors
Temperature is no more than 600 DEG C, and cracking reaction occurs after contacting with catalyst for raw material naphtha or lighter hydrocarbons, is not that Pintsch process is anti-
It answers, therefore a large amount of dry gas, CO, CO will not be generated2Deng raw material naphtha or lighter hydrocarbons selectivity under the action of feature catalyst
Ground is converted into the low-carbon alkene and aromatic hydrocarbons of high yield.
(2) compared with the group technology of catalytic pyrolysis and catalytic reforming/or steam cracking, the present invention only needs a set of reaction system
System and a set of separation system, simple and easy, strong operability, do not need be two or more raw materials coupling or two kinds or more
It plants the coupling of technique and increases the separators such as more extractings, absorption.With method provided by the invention, height can be obtained simultaneously
The propylene of yield and the aromatic hydrocarbons of high yield.
(3) higher propylene and aromatics yield can be obtained simultaneously, propene yield can reach 28% after optimizing reaction condition,
The aromatics yield of coproduction simultaneously can reach 24%.
(4) pass through content, the low temperature cracking reaction condition of adjusting and four light dydrocarbon of self-produced carbon of modified metal in optimization catalyst
The measures such as the internal circulating load of hydrocarbon, available suitable product distribution and required purpose product yield.
(5) according to reaction heat effect and product the characteristics of, can neatly couple with other raw materials and/or other techniques.
Detailed description of the invention
Fig. 1 is the method for the present invention process flow diagram, but the present invention is not limited thereto.
The process flow of this method are as follows: raw material naphtha and the mixing of self-produced four light dydrocarbon hydrocarbon of carbon exchange heat and added through heat exchanger
After hot stove heating, into fixed bed reactors.Under the action of feature catalyst, self-produced four light dydrocarbon hydrocarbon of carbon generation alkene oligomerization,
Cyclisation, aromatization generate macromolecular hydrocarbon, simultaneously because exothermic heat of reaction increases oil gas temperature；Naphtha or lighter hydrocarbons absorb big
The heat of amount occurs the reaction such as dehydrogenation, cracking, overlapping, cyclisation and aromatisation, generates the hydro carbons containing target product propylene and aromatic hydrocarbons
Mixture.Hydrocarbon mixture is flowed out from reactor bottom, after heat exchanger and water cooler are cooling, into subsequent separation system, is obtained
To four light dydrocarbon hydrocarbon of the target product propylene of this method, aromatic hydrocarbons and carbon, a part of four light dydrocarbon hydrocarbon of carbon is gone to as product ejector
Tank field, the self-produced four light dydrocarbon hydrocarbon of carbon of another part are recycled back to reactor, directly enter between reactor catalyst bed, or
It is just mixed with raw material before into reactor, enters reactor together.
Specific embodiment
Below with reference to embodiment, the present invention is further illustrated, but the present invention is not limited thereto.
Raw material specification
(1) hydrocarbon mixture that test raw material is made of naphtha, carbon four and light dydrocarbon, mixed proportion are respectively 70: 25: 5.Its
Middle naphtha is derived from Yanshan Petrochemical, and property is shown in Table 1；Carbon four is derived from carbon four after the ether of Ningxia Petrochemical catalytic cracking unit, organizes prejudice
Table 2；Light dydrocarbon is derived from the material carbon five of Ningxia Petrochemical Etherification of Light FCC Gasoline.
(2) catalyst model CC-17, appearance are the strip in 2.1mm × 3.2mm butterfly section, long 4~10mm.The model
Catalyst is Huiersanji Green Chemical Science and Technology Co., Ltd., Beijing's production, wherein containing 56.8%ZSM-5,1.5%P2O5, 5.6%
La2O3, 0.46%Fe2O3And the Al of surplus2O3.ZSM-5 molecular sieve is the synthesis of in-situ crystallization method, silica alumina ratio 200.
Embodiment 1
This example is illustrated a kind of in parallel as the low-temperature catalyzed reaction propylene processed of raw material using naphtha or lighter hydrocarbons by experimental data
Produce the implementation result of the process of aromatic hydrocarbons.
Experimental rig is 200mL fixed bed reactors, and feedstock oil and water squeeze into preheating furnace with metering pump respectively, then from anti-
It answers the top of device to enter in fixed bed reactors, reacts the gas mixture of generation through exchanging heat, pressure is controlled by regulating valve, pass through
Condensation and gas-liquid separator, separate the liquid that reaction generates and weighing, gas are measured with wet flow indicator, liquids and gases sampling
It is formed afterwards with gas chromatographic analysis, calculated yield (yield based on raw material naphtha weight).
90g catalyst is loaded in reactor.Raw material oil stream amount is 30g/h, water flow 20g/h.Preheating temperature is 540
DEG C, 520 DEG C of catalyst bed mean temperature, reaction pressure 0.1MPa (gauge pressure).Successive reaction 7 days, daily card material balance, and
It takes 2 cracked gases to do composition analysis, collects 1 liquid and do composition analysis；7 days after reaction, unloads agent and burns calculating coke production
Rate.Table 3 and table 4 are 7 days average datas.
1 naphtha main character of table
| Project | Analyze data |
| Density, g/mL | 0.718 |
| Sulfur content, ppm | 26 |
| Determination of Alkane Content, wt% | 78.4 |
| Naphthene content, wt% | 18.7 |
| Arene content, wt% | 1.8 |
| Olefin(e) centent, wt% | 1.1 |
| Boiling range, DEG C | |
| Initial boiling point | 38 |
| 10% | 58 |
| 50% | 105 |
| 90% | 138 |
| It does | 164 |
Carbon four forms after 2 ether of table
| Title | Volume composition, v% |
| Carbon three | 0.45 |
| Normal butane | 12.62 |
| Iso-butane | 39.23 |
| N-butene | 16.62 |
| Isobutene | 0.84 |
| Anti- butylene | 17.06 |
| Maleic | 12.8 |
| Light dydrocarbon | 0.38 |
| It amounts to | 100 |
The reaction condition and product distribution of 3 embodiment of table
| Test number | Embodiment 1 |
| Catalyst | CC-17 |
| Reaction temperature, DEG C | 520 |
| Reaction pressure, MPa | 0.1 |
| Feed space velocities, h-1 | 0.33 |
| Water vapour ratio, wt% | 66.7 |
| Distribution of reaction products, wt% | |
| Hydrogen | 0.32 |
| Methane | 1.39 |
| Ethane | 2.01 |
| Ethylene | 7.07 |
| Propane | 3.68 |
| Propylene | 27.42 |
| Normal butane | 1.50 |
| Iso-butane | 3.01 |
| N-butene | 1.32 |
| Isobutene | 3.13 |
| Maleic | 1.27 |
| Anti- butylene | 1.34 |
| C5+ aromatic naphtha | 46.48 |
| Coke | 0.06 |
| It amounts to | 100 |
The property of 4 aromatic naphtha of table
| Title | Property |
| Density (20 DEG C), g.cm-3 | 0.7326 |
| Octane number RON | 97.5 |
| Boiling range, DEG C | |
| Fore-running | 38 |
| 10% | 79 |
| 50% | 135 |
| 90% | 175 |
| Each component content, wt% | |
| Benzene content | 11.8 |
| Toluene level | 21.6 |
| Xylene content | 20.9 |
Claims (10)
1. a kind of using naphtha or lighter hydrocarbons as the method for the low-temperature catalyzed reaction propylene co-production aromatic hydrocarbons processed of raw material, including following step
It is rapid:
(1) it gas mixture heat exchange after what raw material naphtha or lighter hydrocarbons and reactor bottom flowed out react and/or directly heats
Reach preheating temperature；
(2) after naphtha or lighter hydrocarbons are mixed with self-produced four light dydrocarbon hydrocarbon of carbon, enter from reactor head；
(3) the olefin component hair under the action of feature catalyst loaded in fixed bed reactors, in self-produced four light dydrocarbon hydrocarbon of carbon
Raw overlapping, cyclisation, aromatization generate macromolecular hydrocarbon, simultaneously because exothermic heat of reaction increases oil gas temperature；Naphtha is light
Hydrocarbon absorbs a large amount of heat, and the reaction such as dehydrogenation, cracking, overlapping, cyclisation and aromatisation occurs, generates and contains target product propylene and virtue
The hydrocarbon mixture of hydrocarbon；
(4) hydrocarbon mixture is flowed out from reactor bottom, into subsequent separation system, ethylene that recycling reaction generates, propylene and
Aromatic hydrocarbons, the four light dydrocarbon hydrocarbon of part carbon for reacting generation is recycled to step (2), into reactor together with raw material.
2. according to the method described in claim 1, it is characterized in that raw material naphtha is straight-run naphtha, catalytic cracking stone brain
One of oil, field condensate, hydrocracked naphtha are a variety of.
3. according to the method described in claim 1, it is characterized in that alkane and ring that raw material lighter hydrocarbons refer to four~carbon of carbon ten
Alkane hydrocarbon mixture as main component.
4. according to the method described in claim 1, it is characterized in that naphtha catalytic cracking reaction propylene mistake in step (3)
Journey needs a large amount of heat, and alkene oligomerization, cyclisation and the aromatization of four light dydrocarbon hydrocarbon of self-produced carbon can release a large amount of heat, pass through
The circulation of self-produced four light dydrocarbon hydrocarbon of carbon carries out two reactions in the same reactor, and aromatization provides for cracking reaction
Heat, energy consumption needed for greatly reducing entire technique.
5. according to the method described in claim 4, it is characterized in that can by adjust the internal circulating load of self-produced four light dydrocarbon hydrocarbon of carbon come
Reaction temperature, and regulation distribution of reaction products are controlled, ideal target product yield is obtained.
6. according to the method described in claim 4, it is characterized in that the internal circulating load of four light dydrocarbon hydrocarbon of self-produced carbon can be 0.01~0.5
Times raw material feed rate.
7. according to method of claim 1, it is characterised in that in step (2) and step (4), self-produced four light dydrocarbon hydrocarbon of the carbon circulation in part
The mode for returning reactor can be and directly enter between reactor catalyst bed, can also before entering the reactor with original
Enter reactor together after material mixing.
8. according to the method described in claim 1, it is characterized in that the reactor be fixed bed reactors, be also possible to fluidize
Bed reactor.
9. according to method of claim 1, it is characterised in that in step (3), catalytic reaction condition in reactor are as follows: reaction temperature
460~540 DEG C, 0.1~0.25MPa of reaction pressure, 0.2~1.5h of weight (hourly) space velocity (WHSV)-1。
10. according to method of claim 1, it is characterised in that can be added in step (1), in raw material naphtha or lighter hydrocarbons appropriate
Vapor, to reduce catalyst coking and deactivation, the weight ratio of water and naphtha is 0.01~0.5.
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Denomination of invention: A method for low-temperature catalytic reaction of naphtha or light hydrocarbons to produce propylene and co produce aromatics Granted publication date: 20201127 Pledgee: Urumqi Bank Co.,Ltd. Hami Branch Pledgor: Beijing Huiersanji Green Chem-Tech Co.,Ltd. Registration number: Y2024980011873 |