CN112500891A - Heavy oil processing method and system - Google Patents
Heavy oil processing method and system Download PDFInfo
- Publication number
- CN112500891A CN112500891A CN202011536755.5A CN202011536755A CN112500891A CN 112500891 A CN112500891 A CN 112500891A CN 202011536755 A CN202011536755 A CN 202011536755A CN 112500891 A CN112500891 A CN 112500891A
- Authority
- CN
- China
- Prior art keywords
- outlet
- gas
- oil
- hydrogen
- methanol
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- 239000000295 fuel oil Substances 0.000 title claims abstract description 79
- 238000003672 processing method Methods 0.000 title description 12
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims abstract description 207
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims abstract description 126
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 91
- 239000001257 hydrogen Substances 0.000 claims abstract description 91
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 91
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 91
- 239000007789 gas Substances 0.000 claims abstract description 80
- 238000005336 cracking Methods 0.000 claims abstract description 69
- 238000000197 pyrolysis Methods 0.000 claims abstract description 68
- 239000002994 raw material Substances 0.000 claims abstract description 68
- 239000003921 oil Substances 0.000 claims abstract description 64
- 238000004517 catalytic hydrocracking Methods 0.000 claims abstract description 62
- 239000000047 product Substances 0.000 claims abstract description 62
- 238000000034 method Methods 0.000 claims abstract description 48
- 150000004945 aromatic hydrocarbons Chemical class 0.000 claims abstract description 44
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 claims abstract description 30
- 238000012545 processing Methods 0.000 claims abstract description 25
- URLKBWYHVLBVBO-UHFFFAOYSA-N Para-Xylene Chemical group CC1=CC=C(C)C=C1 URLKBWYHVLBVBO-UHFFFAOYSA-N 0.000 claims abstract description 24
- 239000002283 diesel fuel Substances 0.000 claims abstract description 20
- OFBQJSOFQDEBGM-UHFFFAOYSA-N Pentane Chemical compound CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 claims abstract description 10
- 239000006227 byproduct Substances 0.000 claims abstract description 10
- 230000002194 synthesizing effect Effects 0.000 claims abstract description 8
- 239000003915 liquefied petroleum gas Substances 0.000 claims abstract description 5
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 86
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 53
- 238000002309 gasification Methods 0.000 claims description 51
- 229910052717 sulfur Inorganic materials 0.000 claims description 47
- 239000011593 sulfur Substances 0.000 claims description 47
- 238000004519 manufacturing process Methods 0.000 claims description 40
- 238000011084 recovery Methods 0.000 claims description 37
- 239000012535 impurity Substances 0.000 claims description 25
- 238000001179 sorption measurement Methods 0.000 claims description 11
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 10
- 238000002407 reforming Methods 0.000 claims description 7
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 6
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 claims description 6
- 239000003034 coal gas Substances 0.000 claims description 5
- 238000000746 purification Methods 0.000 claims description 4
- ZBCBWPMODOFKDW-UHFFFAOYSA-N diethanolamine Chemical compound OCCNCCO ZBCBWPMODOFKDW-UHFFFAOYSA-N 0.000 claims description 3
- 229910052757 nitrogen Inorganic materials 0.000 claims description 3
- 229940087646 methanolamine Drugs 0.000 claims description 2
- 230000001131 transforming effect Effects 0.000 claims description 2
- 125000004435 hydrogen atom Chemical class [H]* 0.000 abstract 1
- 238000009413 insulation Methods 0.000 description 30
- 238000005516 engineering process Methods 0.000 description 29
- 238000006243 chemical reaction Methods 0.000 description 28
- 239000010410 layer Substances 0.000 description 19
- 239000000463 material Substances 0.000 description 19
- 239000000571 coke Substances 0.000 description 14
- 238000004873 anchoring Methods 0.000 description 10
- 238000000926 separation method Methods 0.000 description 10
- 239000003054 catalyst Substances 0.000 description 9
- 229910052751 metal Inorganic materials 0.000 description 9
- 239000002184 metal Substances 0.000 description 9
- 239000012071 phase Substances 0.000 description 9
- 230000000712 assembly Effects 0.000 description 8
- 238000000429 assembly Methods 0.000 description 8
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 8
- 238000006317 isomerization reaction Methods 0.000 description 8
- 229910052760 oxygen Inorganic materials 0.000 description 8
- 239000001301 oxygen Substances 0.000 description 8
- 238000007323 disproportionation reaction Methods 0.000 description 7
- 239000007788 liquid Substances 0.000 description 7
- 238000002156 mixing Methods 0.000 description 7
- 239000007790 solid phase Substances 0.000 description 7
- 239000005864 Sulphur Substances 0.000 description 6
- 238000001833 catalytic reforming Methods 0.000 description 6
- 239000003502 gasoline Substances 0.000 description 6
- 230000008929 regeneration Effects 0.000 description 6
- 238000011069 regeneration method Methods 0.000 description 6
- 239000000725 suspension Substances 0.000 description 6
- 238000010555 transalkylation reaction Methods 0.000 description 6
- 229910000831 Steel Inorganic materials 0.000 description 5
- 239000010959 steel Substances 0.000 description 5
- 238000004227 thermal cracking Methods 0.000 description 5
- LCGLNKUTAGEVQW-UHFFFAOYSA-N Dimethyl ether Chemical compound COC LCGLNKUTAGEVQW-UHFFFAOYSA-N 0.000 description 4
- 238000013461 design Methods 0.000 description 4
- 238000000605 extraction Methods 0.000 description 4
- 238000005984 hydrogenation reaction Methods 0.000 description 4
- 239000003208 petroleum Substances 0.000 description 4
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 3
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical compound CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 description 3
- 230000000274 adsorptive effect Effects 0.000 description 3
- 230000008901 benefit Effects 0.000 description 3
- 239000003245 coal Substances 0.000 description 3
- 239000011280 coal tar Substances 0.000 description 3
- 238000004939 coking Methods 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 150000002431 hydrogen Chemical class 0.000 description 3
- 239000012774 insulation material Substances 0.000 description 3
- 239000002245 particle Substances 0.000 description 3
- 239000002006 petroleum coke Substances 0.000 description 3
- 239000002356 single layer Substances 0.000 description 3
- 239000008096 xylene Substances 0.000 description 3
- YNQLUTRBYVCPMQ-UHFFFAOYSA-N Ethylbenzene Chemical compound CCC1=CC=CC=C1 YNQLUTRBYVCPMQ-UHFFFAOYSA-N 0.000 description 2
- 229910021536 Zeolite Inorganic materials 0.000 description 2
- 238000004364 calculation method Methods 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 230000006315 carbonylation Effects 0.000 description 2
- 238000005810 carbonylation reaction Methods 0.000 description 2
- 239000011335 coal coke Substances 0.000 description 2
- 238000005261 decarburization Methods 0.000 description 2
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
- 238000000895 extractive distillation Methods 0.000 description 2
- 238000005194 fractionation Methods 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- NJPPVKZQTLUDBO-UHFFFAOYSA-N novaluron Chemical compound C1=C(Cl)C(OC(F)(F)C(OC(F)(F)F)F)=CC=C1NC(=O)NC(=O)C1=C(F)C=CC=C1F NJPPVKZQTLUDBO-UHFFFAOYSA-N 0.000 description 2
- 238000005191 phase separation Methods 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- 229920006395 saturated elastomer Polymers 0.000 description 2
- 239000002002 slurry Substances 0.000 description 2
- 239000008247 solid mixture Substances 0.000 description 2
- 239000002904 solvent Substances 0.000 description 2
- 238000003860 storage Methods 0.000 description 2
- 230000007704 transition Effects 0.000 description 2
- 239000010457 zeolite Substances 0.000 description 2
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 1
- 239000005977 Ethylene Substances 0.000 description 1
- 229910000990 Ni alloy Inorganic materials 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 1
- 125000003118 aryl group Chemical group 0.000 description 1
- DALDUXIBIKGWTK-UHFFFAOYSA-N benzene;toluene Chemical compound C1=CC=CC=C1.CC1=CC=CC=C1 DALDUXIBIKGWTK-UHFFFAOYSA-N 0.000 description 1
- 239000011449 brick Substances 0.000 description 1
- -1 carbon primary alcohol Chemical class 0.000 description 1
- 238000005266 casting Methods 0.000 description 1
- 239000004568 cement Substances 0.000 description 1
- VNNRSPGTAMTISX-UHFFFAOYSA-N chromium nickel Chemical compound [Cr].[Ni] VNNRSPGTAMTISX-UHFFFAOYSA-N 0.000 description 1
- 239000002131 composite material Substances 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 239000000356 contaminant Substances 0.000 description 1
- 230000008602 contraction Effects 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005520 cutting process Methods 0.000 description 1
- 230000003111 delayed effect Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000000835 fiber Substances 0.000 description 1
- 238000009472 formulation Methods 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 239000007769 metal material Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 229910000510 noble metal Inorganic materials 0.000 description 1
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000011112 process operation Methods 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 238000005496 tempering Methods 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
- 238000003466 welding Methods 0.000 description 1
Images
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
- C10G69/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process
- C10G69/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only
- C10G69/06—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one step of thermal cracking in the absence of hydrogen
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/22—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of gaseous or liquid organic compounds
- C01B3/24—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of gaseous or liquid organic compounds of hydrocarbons
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
- C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
- C01B3/56—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/15—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively
- C07C29/151—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/17—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by hydrogenation of carbon-to-carbon double or triple bonds
- C07C29/172—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by hydrogenation of carbon-to-carbon double or triple bonds with the obtention of a fully saturated alcohol
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
- C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/0266—Processes for making hydrogen or synthesis gas containing a decomposition step
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/06—Integration with other chemical processes
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/06—Integration with other chemical processes
- C01B2203/061—Methanol production
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/06—Integration with other chemical processes
- C01B2203/062—Hydrocarbon production, e.g. Fischer-Tropsch process
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/12—Feeding the process for making hydrogen or synthesis gas
- C01B2203/1205—Composition of the feed
- C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
- C01B2203/1235—Hydrocarbons
- C01B2203/1252—Cyclic or aromatic hydrocarbons
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Inorganic Chemistry (AREA)
- Combustion & Propulsion (AREA)
- General Health & Medical Sciences (AREA)
- Health & Medical Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention provides a method and a system for processing heavy oil. The method comprises at least the following steps: (1) cracking and gasifying heavy oil: cracking and gasifying heavy oil to obtain at least cracked gas, synthetic gas and cracked oil; (2) hydrocracking of pyrolysis oil: hydrocracking the pyrolysis oil obtained in the step (1) to obtain a product comprising dry gas, low-gas, light naphtha, heavy naphtha and diesel oil; (3) aromatic hydrocarbon combination: taking the heavy naphtha obtained in the step (2) as a raw material, and combining aromatic hydrocarbons to obtain a product containing hydrogen, benzene and paraxylene and byproducts containing liquefied petroleum gas, pentane, raffinate oil and heavy aromatic hydrocarbons; (4) methanol synthesis: taking part of the pyrolysis gas and the synthesis gas obtained in the step (1) as raw materials, and synthesizing methanol to obtain a methanol product; (5) ethanol synthesis: and (2) taking the residual pyrolysis gas and synthesis gas obtained in the step (1) as raw materials, and synthesizing ethanol to obtain an ethanol product.
Description
Technical Field
The invention relates to the field of petrochemical industry, in particular to a heavy oil processing method and system.
Background
Typical technologies of heavy oil processing are divided into two types of decarburization and hydrogenation, wherein the first type of decarburization process represents technologies such as delayed coking and flexible coking, and the technologies are non-hydrogenation processes, so that the generation rate of coke is high, the coke is difficult to use, particularly high-sulfur petroleum coke, and the flexible coking adopts an air gasification mode to produce low-calorific-value gas and is mainly used for power generation, but the utilization efficiency and benefit of the coke are not high; the second type of hydrogenation process represents technologies such as fixed bed residual oil hydrogenation, fluidized bed hydrocracking, suspension bed hydrocracking and the like, which obviously reduces the coke yield, but has high investment and operation cost due to high operation pressure.
Disclosure of Invention
Aiming at the problems of difficult processing of heavy oil, low added value of products, high investment and the like, the invention aims to provide a processing method of heavy oil; the processing method can be used for producing high value-added products such as diesel oil, gasoline blending components, aromatic hydrocarbon, methanol, ethanol and the like, overcomes the problem of difficult processing of heavy oil, and is an integrated processing method for producing aromatic hydrocarbon and ethanol by taking heavy oil or coal tar, coal and petroleum coke as raw materials;
it is another object of the present invention to provide a heavy oil processing system.
In order to achieve the above object, in one aspect, the present invention provides a method for processing heavy oil, wherein the method at least comprises the following steps:
(1) cracking and gasifying heavy oil: cracking and gasifying heavy oil to obtain at least cracked gas, synthetic gas and cracked oil;
(2) hydrocracking of pyrolysis oil: hydrocracking the pyrolysis oil obtained in the step (1) to obtain a product comprising dry gas, low-gas, light naphtha, heavy naphtha and diesel oil;
(3) aromatic hydrocarbon combination: taking the heavy naphtha obtained in the step (2) as a raw material, and combining aromatic hydrocarbons to obtain a product containing hydrogen, benzene and paraxylene and byproducts containing liquefied petroleum gas, pentane, raffinate oil and heavy aromatic hydrocarbons;
(4) methanol synthesis: taking part of the pyrolysis gas and the synthesis gas obtained in the step (1) as raw materials, and synthesizing methanol to obtain a methanol product;
(5) ethanol synthesis: and (2) dividing the residual pyrolysis gas obtained in the step (1) (the pyrolysis gas obtained in the step (1) into two parts, wherein one part is used for preparing the methanol in the step (4), and the other part is used for preparing the ethanol in the step, so that the residual pyrolysis gas refers to the residual pyrolysis gas obtained in the step (1) except for the methanol synthesized in the step (4)) and the synthesis gas which are used as raw materials, and synthesizing the ethanol product by using the ethanol.
According to some embodiments of the present invention, the cracking temperature of the cracking and gasification of the heavy oil in step (1) is 500-650 ℃.
According to some embodiments of the present invention, the cracking pressure of the cracking and gasification of the heavy oil in the step (1) is from atmospheric pressure to 8 Mpa.
According to some embodiments of the present invention, the temperature of the gasification in the cracking and gasification of the heavy oil in step (1) is 1000-1300 ℃.
According to some embodiments of the present invention, the pressure of the gasification in the cracking and gasification of the heavy oil in the step (1) is from atmospheric pressure to 8 Mpa.
According to some embodiments of the present invention, the hydrocracking in the step (2) is a hydrocracking using a fixed bed.
According to some embodiments of the present invention, the hydrocracking in step (2) is performed by using a slurry hydrocracking process (refer to patent application with patent number CN101962571A entitled "coal tar heavy fraction slurry hydrocracking method and system", filed as university of great graduates), and all or part of the diesel oil product in step (2) is recycled in the hydrocracking. The proper fraction can also be selected to be processed by a fixed bed hydrocracking unit, or by a combined suspension bed and fixed bed processing technology.
All or part of the wax oil product and/or the diesel oil product in the step (2) can be recycled in hydrocracking, and the distribution of the products can be adjusted according to market demands in a mode of adjusting the diesel oil circulation amount, so that diesel oil or naphtha can be produced in a large amount.
According to some embodiments of the present invention, the method further comprises using the dry gas and the liquefied gas obtained in the steps (2), (3), (4), (5) as raw materials for cracking and gasifying the heavy oil in the step (1).
According to some specific embodiments of the present invention, the method further comprises producing hydrogen by using the synthesis gas obtained in step (1) as a raw material, and/or performing Pressure Swing Adsorption (PSA) purification on the hydrogen-rich product obtained in step (3) and/or step (5) to obtain hydrogen required for hydrocracking in step (2).
The technology for purifying hydrogen by pressure swing adsorption is a conventional technology in the field, and the specific operation steps are not described in detail in the text.
The hydrogen-rich product is a gaseous product comprising hydrogen and is not pure hydrogen.
According to some specific embodiments of the present invention, the method further comprises removing sulfur and nitrogen-containing impurities from the synthesis gas obtained in step (1) by low-temperature methanol or diethanolamine, and passing the sulfur and nitrogen-containing impurities through a sulfur recovery unit to obtain sulfur and liquid ammonia products; and/or passing the impurities containing sulfur and nitrogen obtained after hydrocracking in the step (2) through a sulfur recovery combined device to obtain sulfur and liquid ammonia products.
According to some embodiments of the present invention, the aromatics combination of step (3) comprises all or part of the technologies of continuous reforming, catalyst regeneration, aromatics extraction, disproportionation and transalkylation, adsorptive separation, isomerization and xylene rectification, wherein the technologies of continuous reforming, catalyst regeneration, disproportionation and transalkylation, adsorptive separation and isomerization can be U.S. UOP (U.S. UOP patent technologies can refer to at least the following 5 patents: 1, patent application of catalytic reforming technology with reference to invention name "method for catalytic reforming with naphtha as feedstock", publication No. CN 1044488A; 2, patent application of catalyst regeneration technology with reference to invention name "method and apparatus for regenerating catalyst particles", publication No. CN 103517761A; 3, disproportionation and transalkylation technology with reference to invention name "method for aromatics selectivity with improved conversion", publication No. CN 101668723A; 4. the adsorption separation technique is referred to patent application entitled "method and apparatus for recovering product by adsorption separation and fractionation", publication No. CN 104159647A; 5. isomerization technology reference is made to patent application entitled "selective xylene isomerization and ethylbenzene conversion" with publication number CN1342631A) or to the patent technology of Axens, france (the Axens patent technology of the french oil company can refer to at least the following 5 patents: 1. catalytic reforming technology reference is made to the patent application entitled "process for catalytic reforming in several side-by-side moving bed reaction zones", publication No. CN 1042559A; 2. catalyst regeneration techniques reference is made to a patent application entitled "regeneration process for aromatic hydrocarbon production or reforming catalyst", publication No. CN 1045411A; 3. disproportionation and transalkylation techniques reference is made to a patent application entitled "process for disproportionation and transalkylation of alkylaromatic hydrocarbons in the presence of two zeolite catalysts", publication No. CN 1164524A; 4. adsorption separation techniques reference is made to the patent application entitled "improved simulated moving bed separation process and apparatus", publication No. CN 1714915A; 5. the isomerization technology refers to a patent application with the title of "a double zeolite catalyst containing VIII group metal and IIIA group metal and application thereof in isomerization of aromatic C8 compound", and the publication number is CN 101340976A. the extraction of aromatic hydrocarbon can adopt the extractive distillation technology of the hospital (refer to a patent application with the title of "a method for separating aromatic hydrocarbon by extractive distillation and a composite solvent used", and the publication number is CN 1393507A).
The aromatics complex may employ equipment known in the art, and according to some embodiments of the present invention, the aromatics complex may employ any of a variety of equipment selected from the group consisting of continuous reforming, xylene fractionation, aromatics extraction, BTX separation, disproportionation and transalkylation, isomerization, and adsorptive separation equipment (i.e., a reforming and aromatics complex, as shown in fig. 2).
The process technologies have abundant performances, mature and reliable technology, high recovery rate of the paraxylene and high purity (> 99.8%). The heavy aromatic hydrocarbon byproduct and/or raffinate oil byproduct obtained in the step (3) can be used as a high-octane gasoline blending component, wherein the raffinate oil byproduct is preferentially used as an ethylene cracking raw material.
According to some embodiments of the present invention, step (4) comprises using part of the pyrolysis gas and the synthesis gas obtained in step (1) as raw materials, purifying and transforming, and then performing methanol synthesis to obtain a methanol product.
In the processing method of the heavy oil, the methanol synthesis in the step (4) can adopt the mature and reliable technology for preparing methanol from various synthesis gases at home and abroad. The synthesis gas product obtained in step (1) can be processed by the process to obtain a methanol product.
The purification in step (4) is a conventional method in the art, but according to some embodiments of the present invention, the purification in step (4) may be performed by low temperature methanol washing or diethanolamine absorption.
The shift described in step (4) is well known in the art and is intended to react a portion of the CO with steam to form H2And regulating the hydrogen-carbon ratio of methanol synthesis.
In the above processing method of heavy oil, the ethanol synthesis technology in step (5) adopts a process of synthesizing ethanol by carbonylation of dimethyl ether, which is developed by both elongation group and university (refer to "research progress of preparing ethanol and mixing high carbon primary alcohol from synthetic gas through coal", author din yunje, coal chemical industry "2018, 46 (1)).
Compared with an acetic acid method, the ethanol technology adopts a non-noble metal catalyst, has small corrosion, no special requirement on equipment materials, small equipment investment, friendly production environment and high safety, and can be used for ordering goods in China. The synthetic reaction path is as follows: an enterprise in Shaanxi is the first enterprise in the world to produce ethanol by adopting the route.
In the invention, the ethanol preparation in the step (5) adopts the byproduct methanol from the synthesis gas prepared in the step (4), so the raw materials are low in price and the economic benefit is better.
According to an embodiment of the present invention, the above-mentioned method for processing heavy oil further comprises the steps of: using pyrolysis gas obtained by cracking the heavy oil or gasifying the heavy oil in the step (1) as a raw material to produce hydrogen to obtain sulfur and nitrogen-containing impurities, and obtaining sulfur and liquid ammonia products through a sulfur recovery combined device; and/or hydrocracking the cracked oil obtained in the step (2) to obtain sulfur and nitrogen-containing impurities, and obtaining sulfur and liquid ammonia products through a sulfur recovery combined device.
The sulfur recovery integrated unit is a unit well known in the art, and is generally 2 or 3 units in sulfur recovery, solvent regeneration and sour water stripping. Collectively referred to as a sulfur recovery unit or a sulfur unit.
The sulphur recovery unit may be a sulphur recovery unit as is conventional in the art. In the invention, the part of impurities such as sulfur, nitrogen and the like in the raw material heavy oil entering the pyrolysis oil is converted in the pyrolysis oil hydrocracking process, the part of impurities entering the pyrolysis gas is separated in the hydrogen production process, and then sulfur and liquid ammonia products can be prepared by a sulfur recovery combination device, so that the economic value is increased, and the environmental pollution is reduced.
In another aspect, the present invention further provides a heavy oil processing system, wherein the system comprises a heavy oil cracking and gasifying device 201, a cracked oil hydrocracking device 202, an aromatics complex 203, a methanol synthesis device 204, an ethanol synthesis device 205, a hydrogen production device 206, and a sulfur recovery complex 207; the heavy oil cracking and gasifying device 201 is respectively connected with a cracked oil hydrocracking device 202, a hydrogen production device 206, a methanol synthesis device 204 and an ethanol synthesis device 205 through pipelines, the cracked oil hydrocracking device 202 is respectively connected with an aromatic hydrocarbon combination device 203, a sulfur recovery device 207 and the hydrogen production device 206 through pipelines, the aromatic hydrocarbon combination device 203, the methanol synthesis device 204 and the ethanol synthesis device 205 are respectively connected with the hydrogen production device 206 through pipelines, the methanol synthesis device 204 is connected with the ethanol synthesis device 205 and the hydrogen production device 206 through pipelines, the ethanol synthesis device 205 is connected with the hydrogen production device 206 through pipelines, and the hydrogen production device 206 is connected with the sulfur recovery device 207 through pipelines.
According to some embodiments of the present invention, the heavy oil cracking and gasifying device 201 comprises a heavy oil inlet 211, a cracked gas outlet 212 and a cracked oil outlet 213; the pyrolysis oil hydrocracking unit 202 comprises a pyrolysis oil hydrocracking unit raw material inlet 221, a pyrolysis oil hydrocracking unit hydrogen inlet 222, a light naphtha outlet 223, a heavy naphtha outlet 224, a diesel oil outlet 225 and a pyrolysis oil hydrocracking unit impurity outlet 226; the aromatics complex 203 comprises an aromatics complex feedstock inlet 231, an aromatics complex hydrogen outlet 232, a byproduct outlet 233, a benzene outlet 234, a para-xylene outlet 235, and a heavy aromatics outlet 236; the methanol synthesis unit 204 comprises a methanol synthesis unit raw material inlet 241, a methanol synthesis unit hydrogen outlet 242 and a methanol outlet 243; the ethanol synthesis unit 205 comprises an ethanol synthesis unit feedstock inlet 251, a methanol inlet 252, an ethanol synthesis unit hydrogen outlet 253, and an ethanol outlet 254; the hydrogen production device 206 comprises a hydrogen production device raw material inlet 261, a coal gas raw material inlet 262, a hydrogen production device hydrogen outlet 263 and a hydrogen production device impurity outlet 264; the sulphur recovery unit 207 comprises a recovery unit feedstock inlet 271, a sulphur recovery unit contaminant feedstock inlet 272, a sulphur outlet 273 and a liquid ammonia outlet 274.
According to some embodiments of the present invention, the cracked gas outlet 212 of the heavy oil cracking and gasifying device 201 is connected to the methanol synthesis device raw material inlet 241 of the methanol synthesis device 204, the ethanol synthesis device raw material inlet 251 of the ethanol synthesis device 205, and the coal gas raw material inlet 262 of the hydrogen production device 206 through pipelines, respectively; the pyrolysis oil outlet 213 is connected with a pyrolysis oil hydrocracking unit raw material inlet 221 of the pyrolysis oil hydrocracking unit 202 through a pipeline; a heavy naphtha outlet 224 of the pyrolysis oil hydrocracking unit 202 is connected with an aromatics complex feedstock inlet 231 of the aromatics complex 203 through a pipeline; the cracked oil hydrocracking unit impurity outlet 226 is connected with a sulfur recovery unit impurity raw material inlet 272 of the sulfur recovery unit 207 through a pipeline; the arene combination unit hydrogen outlet 232 of the arene combination unit 203, the methanol synthesis unit hydrogen outlet 242 of the methanol synthesis unit 204, and the ethanol synthesis unit hydrogen outlet 253 of the ethanol synthesis unit 205 are respectively connected with a hydrogen production unit raw material inlet 261 of the hydrogen production unit 206 through pipelines; a methanol outlet 243 of the methanol synthesis device 204 is connected with a methanol inlet 252 of the ethanol synthesis device 205 through a pipeline; the hydrogen production device hydrogen outlet 263 of the hydrogen production device 206 is connected with the recovery device raw material inlet 271 of the sulfur recovery device 207 through a pipeline; the hydrogen plant impurity outlet 264 of the hydrogen plant 206 is connected to the cracked oil hydrocracking plant hydrogen inlet 222 of the cracked oil hydrocracking plant 202 by a pipe.
According to some embodiments of the invention, hydrogen-producing means 206 comprises a pressure swing adsorption unit.
According to some embodiments of the invention, the sulphur recovery unit 207 comprises a pressure swing adsorption unit.
The apparatus 201 for cracking and gasifying heavy oil may be a device known in the art (for example, may be a fluidized bed technology), and according to some embodiments of the present invention, the apparatus includes a cylindrical housing having a hollow reaction chamber, the housing includes a housing body and an insulating lining disposed on an inner wall of the housing body, the reaction chamber has, in order from top to bottom:
the device comprises a cracking section, a gas-phase separation section and a gas-phase separation section, wherein a raw material inlet is formed in the side wall of the upper part of the cracking section, and a gas-phase outlet is formed in the top end of the cracking section;
the side wall of the temperature adjusting section is provided with a steam inlet;
the gasification section, be provided with the oxygen entry on the lateral wall of gasification section, the bottom of gasification section is provided with the solid phase export.
According to some specific embodiments of the present invention, the heat insulation liner includes a heat insulation layer, a plurality of anchoring nails and a plurality of support rings, the plurality of anchoring nails are uniformly distributed on the inner wall surface of the shell body, the plurality of support rings are sequentially spaced on the inner wall of the shell body from top to bottom, the heat insulation layer is formed by pouring a heat insulation material, and the plurality of anchoring nails and the plurality of support rings are embedded in the heat insulation layer.
According to some embodiments of the invention, the thermal insulation layer is a single-layer tortoiseshell-free net structure.
According to some specific embodiments of the present invention, a metal lining is sleeved on the inner wall of the thermal insulation lining of the cracking section and the temperature adjusting section.
According to some embodiments of the invention, the inner diameter of the temperature regulating section is smaller than the inner diameter of the cracking section and the inner diameter of the gasification section.
According to some specific embodiments of the present invention, a cyclone separator is further disposed in the cracking section, the cyclone separator includes a separator body and a material delivery pipe, the separator body includes a cylindrical portion and a conical portion disposed below the cylindrical portion, a connection pipe connected to the gas phase outlet is disposed at a top end of the cylindrical portion, a gas-solid mixture inlet is disposed on a side wall of the cylindrical portion, the material delivery pipe is connected to a bottom end of the conical portion and extends downward to the temperature adjusting section, and a discharge outlet is disposed at a bottom end of the material delivery pipe.
According to some embodiments of the present invention, the inner wall of the cylindrical portion and the inner wall of the conical portion are provided with wear-resistant linings, and the discharge port of the feeding pipe is provided with a flap.
According to some specific embodiments of the present invention, a plurality of heat exchange assemblies for absorbing heat energy in the cracking section are further disposed in the cracking section, and the plurality of heat exchange assemblies are disposed below the separator body.
According to some specific embodiments of the present invention, the heat exchange assembly includes two tube boxes and a plurality of single-pass heat exchange tubes connected in parallel between the two tube boxes, and the two tube boxes are respectively connected with a tube pass liquid conveying pipe, and the conveying pipe penetrates through a side wall of the shell.
According to some specific embodiments of the present invention, the raw material inlet, the gas phase outlet, the steam inlet, the oxygen inlet and the solid phase outlet on the shell are all provided with an outer sleeve structure with a heat insulation lining.
In summary, the invention provides a method and a system for processing heavy oil. The method of the invention has the following advantages:
in the heavy oil processing method provided by the invention, the processing route comprises the processes of heavy oil cracking or heavy oil gasification, cracked oil hydrocracking, aromatic hydrocarbon combination, methanol synthesis, ethanol synthesis and the like, and main products comprise diesel oil, mixed aromatic hydrocarbon, methanol, ethanol and the like. Raw materials and products are mutually supplied among all processes in the processing flow, the types of low-value products are reduced, storage and transportation facilities are optimized, and storage and transportation investment is reduced. The product has concentrated types and high added value. The traditional heavy oil processing mode is broken through, a new method for processing the heavy oil is provided by taking the step (1) as a technical core, the processing means is flexible, and the distribution of each product can be flexibly allocated according to market needs: the high yield of diesel oil, high yield of gasoline, high yield of aromatic hydrocarbon or high yield of methanol can be realized by a simpler means.
In the heavy oil processing system provided by the invention, materials are mutually supplied among devices, so that organic combination is realized, no emission pollution is caused, and the maximum value of various materials is realized.
The processing method and the system for the heavy oil can produce high-value-added products such as diesel oil, gasoline blending components with high octane number, aromatic hydrocarbon, methanol, ethanol and the like, overcome the problem of difficult processing of the heavy oil, greatly improve the economic value of petrochemical products, and flexibly distribute the products according to market requirements, thereby being a novel integrated processing method and a novel integrated processing system for producing the aromatic hydrocarbon and the ethanol by taking the heavy oil or coal tar, coal and petroleum coke as raw materials.
Drawings
FIG. 1 is a schematic diagram of a system connection relationship in embodiment 1 of the present invention;
FIG. 2 is a schematic diagram of an aromatics complex;
FIG. 3 is a schematic structural diagram of a heavy oil cracking and gasifying apparatus according to the present invention;
FIG. 4 is a cross-sectional view taken along line B-B of FIG. 3;
FIG. 5 is a schematic view of the construction of the thermal liner of the present invention;
fig. 6 is a schematic view of an outer jacket structure of the present invention.
Description of reference numerals:
201. a heavy oil cracking and gasifying device; 10. A housing;
11. a housing body; 111. An upper end enclosure;
112. a barrel; 113. A lower end enclosure;
12. a thermal insulating liner; 121. A thermal insulation layer;
122. anchoring nails; 123. A support ring;
20. a reaction chamber; 21. A cracking section;
22. a temperature adjusting section; 23. A gasification stage;
24. a transition section; 31. A raw material inlet;
32. a gas phase outlet; 33. A steam inlet;
34. an oxygen inlet; 35. A solid phase outlet;
36. a dry gas inlet; 40. A cyclone separator;
41. a cylindrical portion; 42. A conical section;
43. a delivery pipe; 44. Wing cutting;
45. hanging; 46. A support structure;
50. a heat exchange assembly; 51. A pipe box;
52. a heat exchange pipe; 53. A tube side liquid conveying pipe;
60. a support assembly; 61. A support beam;
62. a support pedestal; 70. An outer sleeve structure;
71. a thermally insulated liner tube; 72. An outer sleeve;
80. a skirt.
Detailed Description
The following detailed description is provided for the purpose of illustrating the embodiments and the advantageous effects thereof, and is not intended to limit the scope of the present disclosure.
Example 1
A heavy oil processing system as shown in fig. 1, comprising:
a heavy oil cracking and gasifying device 201, a cracked oil hydrocracking device 202, an aromatic hydrocarbon combination device 203, a methanol synthesis device 204, an ethanol synthesis device 205, a hydrogen production device 206 at least comprising pressure swing adsorption equipment, and a sulfur recovery device 207;
the heavy oil cracking and gasifying device 201 comprises a heavy oil inlet 211, a cracked gas outlet 212 and a cracked oil outlet 213;
the pyrolysis oil hydrocracking unit 202 comprises a pyrolysis oil hydrocracking unit raw material inlet 221, a pyrolysis oil hydrocracking unit hydrogen inlet 222, a light naphtha outlet 223, a heavy naphtha outlet 224, a diesel oil outlet 225, a pyrolysis oil hydrocracking unit impurity outlet 226,
the aromatics complex 203 includes an aromatics complex feed inlet 231, an aromatics complex hydrogen outlet 232, a byproduct outlet 233, a benzene outlet 234, a para-xylene outlet 235, and a heavy aromatics outlet 236.
The methanol synthesis unit 204 includes a methanol synthesis unit raw material inlet 241, a methanol synthesis unit hydrogen outlet 242, and a methanol outlet 243.
The ethanol synthesis unit 205 comprises an ethanol synthesis unit feedstock inlet 251, a methanol inlet 252, an ethanol synthesis unit hydrogen outlet 253, and an ethanol outlet 254.
The hydrogen plant 206 includes a hydrogen plant feedstock inlet 261, a coal gas feedstock inlet 262, a hydrogen plant hydrogen outlet 263, and a hydrogen plant impurity outlet 264.
The sulfur recovery device 207 comprises a recovery device raw material inlet 271, a sulfur recovery device impurity raw material inlet 272, a sulfur outlet 273, and a liquid ammonia outlet 274.
As shown in fig. 3 to 6, the pyrolysis gasification reactor 201 provided by the present invention has a shell 10, the shell 10 is cylindrical and has a hollow reaction chamber 20, the shell 10 includes a shell body 11 and a heat insulation lining 12 disposed on an inner wall of the shell body 11, the reaction chamber 20 has a pyrolysis section 21, a temperature adjustment section 22 and a gasification section 23 sequentially disposed from top to bottom; a raw material inlet 31 is arranged on the side wall of the upper part of the cracking section 21, and a gas phase outlet 32 is arranged at the top end of the cracking section 21; a steam inlet 33 is arranged on the side wall of the temperature adjusting section 22; an oxygen inlet 34 is arranged on the side wall of the gasification section 23, and a solid phase outlet 35 is arranged at the bottom end of the gasification section 23.
The pyrolysis gasification reactor 201 provided by the invention arranges the pyrolysis process and the gasification process in one reactor, heavy oil enters the reaction chamber 20 from the upper part of the pyrolysis section 21, then the heavy oil falls in the pyrolysis section, light components in the heavy oil volatilize into oil gas in the falling process, and heavy components condense to form coke; after falling into the gasification section 23, the coke is subjected to a gasification reaction to generate synthesis gas, the synthesis gas flows upwards to exchange heat with descending heavy oil drops, heat is provided for thermal cracking of the heavy oil, the synthesis gas is finally discharged from the gas phase outlet 32, and the residual fine coke particles continuously fall and are finally discharged from the solid phase outlet 35. Thus, the pyrolysis gasification reactor 201 provided by the invention can provide the heat energy released by the coke gasification reaction for the thermal cracking reaction of the heavy oil, the heat energy is reasonably utilized, and the energy consumption is reduced; in addition, the pyrolysis gasification reactor 201 provided by the invention integrates the pyrolysis reaction and the gasification reaction of coke in one reactor, thereby meeting the special process operation requirements of high temperature and short flow, and meanwhile, the pyrolysis gasification reactor 201 provided by the invention has a compact equipment structure and saves the equipment investment.
The pyrolysis gasification reactor 201 provided by the invention is further provided with the temperature adjusting section 22 between the pyrolysis section 21 and the gasification section 23, and the temperature of the synthesis gas entering the pyrolysis section 21 from the gasification section 23 can be controlled through the temperature adjusting section 22, so that the temperature in the pyrolysis section 21 is prevented from being too high, and the temperature in the pyrolysis section 21 is ensured to be the temperature most suitable for the heavy oil thermal cracking reaction.
The shell 10 of the cracking gasification reactor 201 provided by the invention is provided with the heat insulation lining 12 to form a cold wall structure, so that the operation requirement of a high-temperature reactor can be met, and the local temperature in the reaction cavity 20 can reach 1200 ℃; meanwhile, the heat insulation lining 12 can effectively isolate the heat in the reaction cavity 20 from being transferred outwards, so that the actual service temperature of the shell body 11 is far lower than the temperature in the reaction cavity 20, the wall temperature of the shell body 11 can be guaranteed not to exceed the service temperature limit of steel, and meanwhile, the requirement of high temperature resistance of the material selected for the shell body 11 is also reduced, namely, the shell body 11 can meet the service requirement by selecting the material for the pressure container commonly used in engineering.
In an alternative example of the present invention, the thermal insulation liner 12 includes a thermal insulation layer 121, anchoring nails 122 and support rings 123, the anchoring nails 122 are uniformly distributed on the inner wall surface of the shell body 11, the anchoring nails 122 are V-shaped and have a bottom and two support portions, the bottom of the anchoring nails 122 is fixedly connected to the inner wall of the shell body 11, the support rings 123 are sequentially arranged on the inner wall of the shell body 11 from top to bottom at intervals, the support rings 123 are horizontally arranged circular ring plates, the outer edge of the support rings 123 is fixedly connected to the inner wall of the shell body 11, the thermal insulation layer 121 is formed by pouring a thermal insulation material, and the anchoring nails 122 and the support rings 123 are embedded inside the thermal insulation layer 121, so that the thermal insulation layer 121 is fixed on the shell body 11 by the anchoring nails 122, and the support rings 123 can also vertically support the thermal insulation layer 121, thereby preventing the thermal insulation layer 121 from.
In an alternative example of the present invention, the thermal insulation layer 121 may be a mixed casting material or a special-shaped brick of a "high-alumina thermal insulation material" and a "high-temperature cement" which are mature in engineering, and the specific formulation and the thickness of the thermal insulation layer may be determined by "heat transfer calculation" according to the specific operating conditions of the equipment.
In an alternative example, the housing body 11 is a metal housing body, the anchor pins 122 and the support rings 123 may be made of heat-insulating Cr-Mo steel material or stainless steel material, and the anchor pins 122 and the support rings 123 are fixedly connected to the inner wall of the housing body 11 by welding.
In an alternative embodiment of the present invention, the housing 10 is fixedly installed by the skirt 80, and the structure of the skirt 80 may be the prior art, which will not be described in detail herein.
In an alternative example of the present invention, the thermal insulation layer 121 is of a single-layer structure without a tortoise-shell net, that is, the thermal insulation layer 121 is uniformly filled with high-temperature resistant metal fibers, so as to improve the peeling resistance of the thermal insulation layer. It should be noted that the single-layer tortoise-shell-free net structure is a mature technology in engineering and is widely applied at present.
In an optional example of the present invention, a metal liner 124 is further disposed on an inner wall of the heat insulating layer 121 located in the cracking section 21 and the temperature adjusting section 22, and the metal liner can prevent materials in the reaction chamber 20 from directly contacting the heat insulating layer 121, so as to improve the service life of the heat insulating layer 121. The material of the metal lining barrel can be selected from high-temperature resistant metal materials, such as high-temperature resistant chromium-nickel alloy and the like.
In an alternative embodiment of the present invention, the inner diameter of the temperature adjusting section 22 is smaller than the inner diameter of the cracking section 21 and the inner diameter of the gasification section 23, so as to increase the time and flow for the syngas to enter the cracking section 21 from the gasification section 23, and further decrease the temperature of the syngas entering the cracking section 21, and accordingly decrease the temperature in the cracking section 21, which makes it more suitable for the thermal cracking reaction of heavy oil.
In an alternative embodiment of the invention, the upper and lower ends of the temperature control section 22 are connected to the cracking section 21 and the gasification section 23, respectively, via a transition section 24.
In the present invention, the side wall of the temperature adjusting section 22 is further provided with a steam inlet 33, and saturated steam can not only lower the temperature of the synthesis gas, but also be used for the gasification reaction of coke.
In an alternative example, two steam inlets 33 are provided on the sidewall of the temperature adjusting section 22, and the two steam inlets 33 are spaced apart in the vertical direction.
In an alternative embodiment of the invention, the height of the cracking section 21, the height of the tempering section 22 and the height of the gasification section 23 can be determined by process calculations
In an optional example of the present invention, a cyclone separator 40 is further disposed in the cracking section 21, the cyclone separator 40 is located at the top of the cracking section 21, the cyclone separator 40 includes a separator body 47 and a material conveying pipe (dipleg) 43, the separator body has a cylindrical portion 41 and a conical portion 42 disposed below the cylindrical portion 41, a connection pipe 411 connected to the gas phase outlet 32 is disposed at the top end of the cylindrical portion 41, a gas-solid mixture inlet 48 is disposed on the side wall of the cylindrical portion 41, the material conveying pipe 43 is connected to the bottom end of the conical portion 42 and extends downward to the temperature adjusting section 22, and a discharge port 431 is disposed at the bottom end of the material conveying pipe 43. The cyclone separator 40 can separate the small particle coke carried in the synthesis gas, which not only can improve the purity of the gas discharged from the gas phase outlet 32, but also can convey the separated coke back to the gasification stage 23 through the material conveying pipe 43 to continue the gasification reaction, thereby improving the gasification rate of the coke.
In an alternative embodiment of the present invention, wear resistant linings 49 are provided on both the inner wall of the cylindrical portion 41 and the inner wall of the conical portion 42 to improve the service life of the cyclone 40, and a flap 44 is provided at the outlet of the delivery pipe 43 to allow coke to enter the gasification zone 23 at a fixed angle (to form a solid phase level).
In an alternative embodiment of the present invention, the cylindrical portion 41 and the conical portion 42 are made of high temperature resistant steel plates, and the feed delivery pipe 43 is made of high temperature resistant steel pipe.
In the present invention, the cyclone separator 40 is disposed in the cracking section 21 by a high temperature resistant hanger 45, one end of the hanger 45 is connected to the upper head 111, and the other end of the hanger 45 is connected to the cylindrical portion. The conical section 42 and the feed conveyor 43 are fixed to the inner wall of the cracking section 21 by radial support structures 46, and the radial support structures 46 can effectively ensure free expansion and contraction at high temperature.
In an alternative example of the present invention, a plurality of heat exchange assemblies 50 for absorbing heat are further disposed in the cracking section 21, and the plurality of heat exchange assemblies 50 are disposed below the separator body (conical portion 43). Heat exchange assembly 50 can absorb the heat in pyrolysis section 21, further prevents that the reaction temperature in pyrolysis section 21 is too high, guarantees going on smoothly of heavy oil thermal cracking reaction, and simultaneously, heat exchange assembly 50 can also effectively utilize the heat in pyrolysis section 21 for heat other raw materials in the petrochemical industry production.
In an alternative example, the heat exchange assembly 50 includes two tube boxes 51 and a plurality of one-way heat exchange tubes 52 connected in parallel between the two tube boxes 51, wherein the two tube boxes 51 are respectively connected with tube side liquid conveying tubes 53, and the tube side liquid conveying tubes 53 penetrate through the side wall of the shell 10. Compared to conventional heat exchangers, the heat exchange assembly 50 of the present invention does not have a conventional shell-side cylinder.
In an alternative example, the tube box 51, the heat exchange tube 52 and the tube pass liquid conveying tube 53 are made of high temperature resistant materials.
Of course, the heat exchange assembly 50 may also be in the form of a spiral tube or other form, as long as the heat in the cracking section 21 can be utilized.
In an optional example of the present invention, a plurality of heat exchange units are disposed in the cracking section 21, the heat exchange units are sequentially disposed from top to bottom, four heat exchange assemblies 50 are disposed in each heat exchange unit, the four heat exchange assemblies 50 are uniformly distributed along the circumference of the cracking section 21, intervals are provided between the four heat exchange assemblies 50, and the material conveying pipe 43 of the cyclone separator 40 passes through the intervals between the heat exchange assemblies 50.
In an alternative example of the present invention, the tube box 51 of the heat exchange assembly 50 is fixed in the cracking section 21 by a support assembly 60, the support assembly 60 has a plurality of support beams 61, an inner convex support pedestal 62 is provided on the inner wall of the cracking section 21, and both ends of the support beams 61 overlap the corresponding support pedestals 62.
In an alternative example of the present invention, the raw material inlet 31, the gas phase outlet 32, the steam inlet 33, the oxygen inlet 34, and the solid phase outlet 35 on the shell 10 are all provided with an outer sleeve structure 70 with a thermal insulation liner, specifically, the structure includes a thermal insulation liner pipe 71 and an outer sleeve 72, the thermal insulation liner pipe 71 is connected with the thermal insulation liner 12 of the shell 10, the outer sleeve 72 is sleeved outside the thermal insulation liner pipe 71 and connected with the shell body 11, and the outer sleeve structure 70 with the thermal insulation liner can further ensure that the portion of the shell 10 connected with the outside can also bear the high temperature in the reaction chamber 20, thereby further ensuring the service life of the whole pyrolysis gasification reactor 201.
In an alternative example of the present invention, an outer sleeve structure 70 is also provided at the interface of the tube-side liquid conveying tube 53 of the heat exchange assembly 50 and the shell 10.
In an alternative embodiment of the present invention, the side wall of the gasification stage 23 is further opened with a dry gas inlet 36, and the oxygen inlet 34 can also be used for conveying saturated steam.
In an alternative example, steam nozzles are installed at both the steam inlet 33 and the oxygen inlet 34.
In an alternative example of the present invention, the casing 10 may be provided with a plurality of raw material inlets 31, and the plurality of raw material inlets 31 are uniformly distributed along the circumferential direction of the casing 10.
In an alternative example of the present invention, the shell body 11 includes an upper head 111, a cylinder 112 and a lower head 113 which are sequentially arranged from top to bottom and are hermetically connected, and the inner walls of the upper head 111, the cylinder 112 and the lower head 113 are covered with the thermal insulation lining 12.
In an alternative example, the upper head 111, the cylinder 112 and the lower head 113 are welded together.
In an alternative embodiment of the present invention, the pyrolysis gasification reactor 201 has a local maximum design temperature of 1200 ℃, a design pressure of 1.0MPa, a tube side design pressure of 6.0MPa for the heat exchange assembly 40, a tube side liquid (medium) may be heavy oil, naphtha, diesel, methane, hydrogen, oxygen, etc., and the tube box 51 has a diameter of 1200 mm
The upper end enclosure 111 of the cracking gasification reactor 201 adopts a ball end enclosure, and the lower end enclosure 112 is a flanging cone end enclosure; the design temperature of the metal of the shell body 11 of the pyrolysis gasification reactor 201 is 300 ℃, and the whole is made of a steel plate for a pressure vessel.
In an alternative embodiment of the present invention, the internals of the pyrolysis gasification reactor 201, such as the cyclone separator 40, the heat exchange assembly 40, the refractory hanger 45, and the support structure 46, are installed before the upper head 111 and the shell 112 are welded.
The method of this embodiment is specifically as follows:
hydrocracking of pyrolysis oil adopts a suspension bed hydrocracking process technology, combining aromatic hydrocarbon adopts a complete set technology of Axens company, methanol adopts a technology of preparing methanol by using synthetic gas of UK DAVY, and ethanol adopts a prolonged middle-aged dimethyl ether carbonylation technical route.
Heavy oil is used as a raw material, and the cracked oil is obtained by cracking (500-650 ℃, normal pressure-8 MPa) or gasifying (1000-1300 ℃, normal pressure-8 MPa) the heavy oil. The cracking oil is used as a raw material for VCC suspension bed hydrocracking, and main products of a cracking oil hydrocracking device comprise light naphtha, heavy naphtha and diesel oil. Wherein the heavy naphtha is used as the raw material of the aromatic hydrocarbon combination unit, the light naphtha is used as the raw material of the heavy oil cracking and gasifying device or sold as the product, and the diesel oil is used as the diesel oil blending component product and sent out of the device.
The heavy naphtha enters a continuous reforming device of an aromatic hydrocarbon combination unit to carry out catalytic reforming reaction (as shown in figure 2), and the reaction conditions of the catalytic reforming are 490-530 ℃ and 0.3-0.4 MPa. The main product is reformate (C6+), which is processed by other devices of the aromatics complex, namely an aromatics extraction device, a disproportionation and benzene-toluene separation device, an adsorption separation device and an isomerization device. The product of the aromatics complex comprises: hydrogen-containing gas, liquefied petroleum gas, pentane, raffinate oil, benzene, p-xylene and heavy aromatic hydrocarbon products. Wherein, the heavy aromatic hydrocarbon product is sold; the liquefied petroleum gas, pentane and raffinate oil products are used as raw materials of a heavy oil cracking and gasifying device or sold as products.
The hydrogen-containing gas of the aromatic hydrocarbon combination unit and the sulfur-containing low-molecular gas (containing hydrogen) of the suspension bed hydrocracking unit are purified by pressure swing adsorption and then supplied to the VCC suspension bed hydrocracking unit for use.
As the content of impurities in the pyrolysis oil is high, the carbon-hydrogen ratio is high, and a large amount of hydrogen needs to be consumed, the hydrogen produced by the device is not enough to meet the requirement of hydrocracking, and the hydrogen production supplement requirement of a hydrogen production device needs to be set, and the hydrogen production device adopts pyrolysis gas as a raw material.
The final products of the whole processing route are diesel oil, gasoline blending components, aromatic hydrocarbon, methanol and ethanol products, and if the principle of producing p-xylene at most is adopted, no diesel oil is produced.
The properties of the diesel product are shown in table 1 below:
TABLE 1 Diesel product Properties
The properties of the benzene product are as follows:
the product meets the technical requirements of petroleum benzene GB/T3405-2011, and the quality indexes are shown in Table 2 below.
TABLE 2 quality index of petroleum benzene (GB/T3405-2011)
Product properties of p-xylene:
meets the index requirements of superior products in the petrochemical industry standard SH1486.1-2008 of the people's republic of China.
The quality indexes of superior petroleum paraxylene (SH1486.1-2008) are shown in the following table 3, and the quality indexes of prepared ethanol are shown in the following table 4.
TABLE 3 quality index of petroleum paraxylene (SH14861-2008) high-class product
TABLE 4 ethanol quality index
The heavy oil processing method and the heavy oil processing system provided by the invention can be used for producing high-value-added products such as diesel oil, aromatic hydrocarbon, (high-octane) gasoline blending components, ethanol and the like, improve the utilization rate and economic value of the traditional heat processing of the heavy oil, and can flexibly distribute the products according to market demands, thereby being a novel integrated processing route and system for the heavy oil, the coal, the aromatic hydrocarbon and the ethanol.
Claims (10)
1. A method for processing heavy oil, wherein the method comprises at least the steps of:
(1) cracking and gasifying heavy oil: cracking and gasifying heavy oil to obtain at least cracked gas, synthetic gas and cracked oil;
(2) hydrocracking of pyrolysis oil: hydrocracking the pyrolysis oil obtained in the step (1) to obtain a product comprising dry gas, low-gas, light naphtha, heavy naphtha and diesel oil;
(3) reforming and aromatic hydrocarbon combination: taking the heavy naphtha obtained in the step (2) as a raw material, and combining aromatic hydrocarbons to obtain products containing hydrogen-rich gas, benzene and paraxylene and byproducts containing dry gas, liquefied petroleum gas, pentane, raffinate oil and heavy aromatic hydrocarbons;
(4) methanol synthesis: taking part of the pyrolysis gas and the synthesis gas obtained in the step (1) as raw materials, and synthesizing methanol to obtain a methanol product (preferably, the step (4) comprises the steps of taking part of the pyrolysis gas and the synthesis gas obtained in the step (1) as raw materials, purifying and transforming the raw materials, and synthesizing methanol to obtain the methanol product);
(5) ethanol synthesis: and (2) taking the residual pyrolysis gas and the synthesis gas obtained in the step (1) as raw materials, synthesizing ethanol to obtain an ethanol product, and simultaneously obtaining tail gas which is hydrogen-rich gas.
2. The method as claimed in claim 1, wherein the cracking temperature of the cracking and gasification of the heavy oil in step (1) is 500-650 ℃; the temperature of gasification is 1000-1300 ℃.
3. The method as claimed in claim 1, wherein the cracking pressure of the heavy oil cracking and gasification of step (1) is normal pressure to 8 Mpa; the gasification pressure is from normal pressure to 8 Mpa.
4. The process of claim 1, wherein the hydrocracking in step (2) is a hydrocracking with a fixed bed.
5. The method of claim 1, wherein the method further comprises using the dry gas and the liquefied gas obtained in steps (2), (3), (4), and (5), and the tail gas of steps (4) and (5) as raw materials for cracking and gasifying the heavy oil of step (1).
6. The process according to claim 1, wherein the process further comprises producing hydrogen by using the synthesis gas obtained in step (1) as a raw material, and/or performing pressure swing adsorption purification on the hydrogen-rich product gas obtained in step (3) and/or step (5) to obtain hydrogen required for hydrocracking in step (2).
7. The process according to claim 1, wherein the process further comprises removing sulfur and nitrogen-containing impurities from the synthesis gas obtained in step (1) by low-temperature methanol or diethanolamine, and passing the sulfur and nitrogen-containing impurities to a sulfur recovery unit to obtain sulfur and liquid ammonia products; and/or passing the impurities containing sulfur and nitrogen obtained after hydrocracking in the step (2) through a sulfur recovery combined device to obtain sulfur and liquid ammonia products.
8. A heavy oil processing system, wherein the system comprises a heavy oil cracking and gasification unit (201), a cracked oil hydrocracking unit (202), an aromatics complex (203), a methanol synthesis unit (204), an ethanol synthesis unit (205), a hydrogen production unit (206), and a sulfur recovery unit (207); the heavy oil cracking and gasifying device (201) is respectively connected with a cracked oil hydrocracking device (202), a hydrogen production device (206), a methanol synthesis device (204) and an ethanol synthesis device (205) through pipelines, the cracked oil hydrocracking device (202) is respectively connected with an aromatic hydrocarbon combination device (203), a sulfur recovery device (207) and the hydrogen production device (206) through pipelines, the aromatic hydrocarbon combination device (203), the methanol synthesis device (204) and the ethanol synthesis device (205) are respectively connected with the hydrogen production device (206) through pipelines, the methanol synthesis device (204) is connected with the ethanol synthesis device (205) and the hydrogen production device (206) through pipelines, the ethanol synthesis device (205) is connected with the hydrogen production device (206) through pipelines, and the hydrogen production device (206) is connected with the sulfur recovery device (207) through pipelines.
9. The system of claim 8, wherein the heavy oil cracking and gasification apparatus (201) comprises a heavy oil inlet (211), a cracked gas outlet (212), and a cracked oil outlet (213); the pyrolysis oil hydrocracking device (202) comprises a pyrolysis oil hydrocracking device raw material inlet (221), a pyrolysis oil hydrocracking device hydrogen inlet (222), a light naphtha outlet (223), a heavy naphtha outlet (224), a diesel oil outlet (225) and a pyrolysis oil hydrocracking device impurity outlet (226); the aromatic hydrocarbon combination unit (203) comprises an aromatic hydrocarbon combination unit raw material inlet (231), an aromatic hydrocarbon combination unit hydrogen outlet (232), a byproduct outlet (233), a benzene outlet (234), a paraxylene outlet (235) and a heavy aromatic hydrocarbon outlet (236); the methanol synthesis device (204) comprises a methanol synthesis device raw material inlet (241), a methanol synthesis device hydrogen outlet (242) and a methanol outlet (243); the ethanol synthesis device (205) comprises an ethanol synthesis device raw material inlet (251), a methanol inlet (252), an ethanol synthesis device hydrogen outlet (253) and an ethanol outlet (254); the hydrogen production device (206) comprises a hydrogen production device raw material inlet (261), a coal gas raw material inlet (262), a hydrogen production device hydrogen outlet (263) and a hydrogen production device impurity outlet (264); the sulfur recovery device (207) comprises a recovery device raw material inlet (271), a sulfur recovery device impurity raw material inlet (272), a sulfur outlet (273) and a liquid ammonia outlet (274).
10. The system of claim 9, wherein the cracked gas outlet (212) of the heavy oil cracking and gasifying device (201) is connected with the methanol synthesis device raw material inlet (241) of the methanol synthesis device (204), the ethanol synthesis device raw material inlet (251) of the ethanol synthesis device (205) and the coal gas raw material inlet (262) of the hydrogen production device (206) through pipelines respectively; the pyrolysis oil outlet (213) is connected with a pyrolysis oil hydrocracking unit raw material inlet (221) of the pyrolysis oil hydrocracking unit (202) through a pipeline; a heavy naphtha outlet (224) of the pyrolysis oil hydrocracking unit (202) is connected with an aromatic hydrocarbon combined unit raw material inlet (231) of the aromatic hydrocarbon combined unit (203) through a pipeline; an impurity outlet (226) of the pyrolysis oil hydrocracking device is connected with an impurity raw material inlet (272) of a sulfur recovery device of the sulfur recovery device (207) through a pipeline; an arene combined device hydrogen outlet (232) of the arene combined device (203), a methanol synthesis device hydrogen outlet (242) of the methanol synthesis device (204) and an ethanol synthesis device hydrogen outlet (253) of the ethanol synthesis device (205) are respectively connected with a hydrogen production device raw material inlet (261) of the hydrogen production device (206) through pipelines; a methanol outlet (243) of the methanol synthesis device (204) is connected with a methanol inlet (252) of the ethanol synthesis device (205) through a pipeline; a hydrogen outlet (263) of the hydrogen production device (206) is connected with a raw material inlet (271) of the sulfur recovery device (207) through a pipeline; an impurity outlet (264) of the hydrogen production device (206) is connected with a hydrogen inlet (222) of the pyrolysis oil hydrocracking device (202) through a pipeline.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202011536755.5A CN112500891A (en) | 2020-12-23 | 2020-12-23 | Heavy oil processing method and system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202011536755.5A CN112500891A (en) | 2020-12-23 | 2020-12-23 | Heavy oil processing method and system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN112500891A true CN112500891A (en) | 2021-03-16 |
Family
ID=74923494
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202011536755.5A Pending CN112500891A (en) | 2020-12-23 | 2020-12-23 | Heavy oil processing method and system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN112500891A (en) |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20130087484A1 (en) * | 2011-10-07 | 2013-04-11 | Uop Llc | Integrated catalytic cracking gasoline and light cycle oil hydroprocessing to maximize p-xylene production |
| WO2018094353A1 (en) * | 2016-11-21 | 2018-05-24 | Saudi Arabian Oil Company | Process and system for conversion of crude oil to petrochemicals and fuel products integrating steam cracking, fluid catalytic cracking, and conversion of naphtha into chemical rich reformate |
| US20190203130A1 (en) * | 2017-12-29 | 2019-07-04 | Lummus Technology Llc | Conversion of heavy fuel oil to chemicals |
| CN110283628A (en) * | 2019-07-10 | 2019-09-27 | 北京石油化工工程研究院 | A kind of cracking gasification reactor |
| CN214457791U (en) * | 2020-12-23 | 2021-10-22 | 北京石油化工工程研究院 | Heavy oil processing system |
-
2020
- 2020-12-23 CN CN202011536755.5A patent/CN112500891A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20130087484A1 (en) * | 2011-10-07 | 2013-04-11 | Uop Llc | Integrated catalytic cracking gasoline and light cycle oil hydroprocessing to maximize p-xylene production |
| WO2018094353A1 (en) * | 2016-11-21 | 2018-05-24 | Saudi Arabian Oil Company | Process and system for conversion of crude oil to petrochemicals and fuel products integrating steam cracking, fluid catalytic cracking, and conversion of naphtha into chemical rich reformate |
| US20190203130A1 (en) * | 2017-12-29 | 2019-07-04 | Lummus Technology Llc | Conversion of heavy fuel oil to chemicals |
| CN110283628A (en) * | 2019-07-10 | 2019-09-27 | 北京石油化工工程研究院 | A kind of cracking gasification reactor |
| CN214457791U (en) * | 2020-12-23 | 2021-10-22 | 北京石油化工工程研究院 | Heavy oil processing system |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101244969B (en) | Continuous aromatization and catalyst regeneration device and method thereof | |
| CN108017496B (en) | Apparatus for producing olefins and aromatic hydrocarbons and method thereof | |
| CN101591562B (en) | Fluid catalytic cracking method and device thereof | |
| CN108017487B (en) | Two-stage reaction method for preparing aromatic hydrocarbon from oxygen-containing compound-containing raw material | |
| CN100534581C (en) | Control of hydrogen in hydrogen-containing streams from hydrogen sources | |
| NO171409B (en) | PROCEDURE FOR THE PREPARATION OF A HYDROGENRIQUE GAS VEDA AUTOTHERMIC REFORM OF A HYDROCARBON-CONTAINED OUTPUT MATERIAL | |
| GB2191214A (en) | Production of higher molecular weight hydrocarbons from methane | |
| CN104140847A (en) | Method for production of high-octane gasoline by modification of Fischer-Tropsch synthetic naphtha | |
| CN104098419B (en) | Coal, natural gas combination preparing light olefins from methanol system and method | |
| CN214457791U (en) | Heavy oil processing system | |
| CN108017490A (en) | Method containing oxygen-containing compound material catalytic cracking aromatic hydrocarbons | |
| CN201280527Y (en) | Aromatic hydrocarbon production equipment | |
| CN108017486B (en) | Method for preparing aromatic hydrocarbon by converting oxygen-containing compound-containing raw material | |
| CN108017489B (en) | Method for preparing aromatic hydrocarbon by catalytic conversion of oxygen-containing compound raw material | |
| CN111056901B (en) | Reaction system and reaction method for preparing aromatic hydrocarbon through catalytic conversion of methanol | |
| US9243189B2 (en) | Conversion of natural gas | |
| CN112500891A (en) | Heavy oil processing method and system | |
| CN111747811B (en) | Process for oxidative coupling of methane | |
| CN101343568A (en) | Method for preparing gasoline with petroleum cracking of dry gas | |
| CN108017488A (en) | The method of alcohol and/or ether catalytic material conversion for preparing arene | |
| CN111100664B (en) | Method for preparing aromatic hydrocarbon by catalytic conversion of methanol | |
| CN111056895B (en) | Partitioned reaction system and reaction method for preparing aromatic hydrocarbon through methanol conversion | |
| CN108017482B (en) | Method for preparing aromatic hydrocarbon by converting raw material containing oxygen-containing compound | |
| RU2776173C1 (en) | Method for producing liquid hydrocarbons using the fischer-tropsch process integrated in petroleum refining plants | |
| CN101759511B (en) | Low olefin-content lighter hydrocarbons are utilized to produce the method for aromatic hydrocarbons |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination |