CN116496813A - Catalytic conversion method for producing C6-C8 light aromatic hydrocarbon - Google Patents
Catalytic conversion method for producing C6-C8 light aromatic hydrocarbon Download PDFInfo
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- 150000004945 aromatic hydrocarbons Chemical class 0.000 title claims abstract description 92
- 238000006243 chemical reaction Methods 0.000 title claims abstract description 88
- 230000003197 catalytic effect Effects 0.000 title claims abstract description 30
- 238000004519 manufacturing process Methods 0.000 title abstract description 11
- 238000004523 catalytic cracking Methods 0.000 claims abstract description 213
- 125000003118 aryl group Chemical group 0.000 claims abstract description 89
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 86
- 238000000926 separation method Methods 0.000 claims abstract description 74
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 claims abstract description 60
- -1 monocyclic aromatic hydrocarbon Chemical class 0.000 claims abstract description 55
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 claims abstract description 54
- 238000000605 extraction Methods 0.000 claims abstract description 43
- 238000000034 method Methods 0.000 claims abstract description 38
- 125000005575 polycyclic aromatic hydrocarbon group Chemical group 0.000 claims abstract description 36
- 239000002994 raw material Substances 0.000 claims abstract description 25
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical compound CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 claims abstract description 18
- 239000008096 xylene Substances 0.000 claims abstract description 18
- 239000003921 oil Substances 0.000 claims description 111
- 239000003054 catalyst Substances 0.000 claims description 72
- 239000007789 gas Substances 0.000 claims description 33
- 230000008569 process Effects 0.000 claims description 22
- 238000004821 distillation Methods 0.000 claims description 20
- 239000001257 hydrogen Substances 0.000 claims description 19
- 229910052739 hydrogen Inorganic materials 0.000 claims description 19
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 15
- 239000000295 fuel oil Substances 0.000 claims description 15
- 239000010724 circulating oil Substances 0.000 claims description 14
- 238000005520 cutting process Methods 0.000 claims description 9
- 239000002904 solvent Substances 0.000 claims description 9
- HXJUTPCZVOIRIF-UHFFFAOYSA-N sulfolane Chemical compound O=S1(=O)CCCC1 HXJUTPCZVOIRIF-UHFFFAOYSA-N 0.000 claims description 9
- IAZDPXIOMUYVGZ-UHFFFAOYSA-N Dimethylsulphoxide Chemical compound CS(C)=O IAZDPXIOMUYVGZ-UHFFFAOYSA-N 0.000 claims description 8
- SECXISVLQFMRJM-UHFFFAOYSA-N N-Methylpyrrolidone Chemical compound CN1CCCC1=O SECXISVLQFMRJM-UHFFFAOYSA-N 0.000 claims description 4
- LCEDQNDDFOCWGG-UHFFFAOYSA-N morpholine-4-carbaldehyde Chemical compound O=CN1CCOCC1 LCEDQNDDFOCWGG-UHFFFAOYSA-N 0.000 claims description 4
- 230000009471 action Effects 0.000 claims description 3
- 239000012528 membrane Substances 0.000 claims description 3
- 238000002156 mixing Methods 0.000 claims description 3
- 238000005899 aromatization reaction Methods 0.000 claims description 2
- 239000003245 coal Substances 0.000 claims description 2
- 238000002407 reforming Methods 0.000 claims description 2
- 239000003079 shale oil Substances 0.000 claims description 2
- 238000004230 steam cracking Methods 0.000 claims description 2
- 230000000274 adsorptive effect Effects 0.000 claims 1
- 238000007700 distillative separation Methods 0.000 claims 1
- 239000000047 product Substances 0.000 description 47
- 239000000203 mixture Substances 0.000 description 22
- 239000002283 diesel fuel Substances 0.000 description 20
- 230000000052 comparative effect Effects 0.000 description 12
- 229930195733 hydrocarbon Natural products 0.000 description 7
- 239000007795 chemical reaction product Substances 0.000 description 6
- 150000001924 cycloalkanes Chemical class 0.000 description 6
- 230000000694 effects Effects 0.000 description 6
- 238000004817 gas chromatography Methods 0.000 description 6
- 239000003502 gasoline Substances 0.000 description 6
- 150000002430 hydrocarbons Chemical class 0.000 description 6
- 239000000571 coke Substances 0.000 description 5
- FYGHSUNMUKGBRK-UHFFFAOYSA-N 1,2,3-trimethylbenzene Chemical compound CC1=CC=CC(C)=C1C FYGHSUNMUKGBRK-UHFFFAOYSA-N 0.000 description 4
- 239000004215 Carbon black (E152) Substances 0.000 description 4
- 238000004458 analytical method Methods 0.000 description 4
- 238000006482 condensation reaction Methods 0.000 description 4
- WOZVHXUHUFLZGK-UHFFFAOYSA-N dimethyl terephthalate Chemical compound COC(=O)C1=CC=C(C(=O)OC)C=C1 WOZVHXUHUFLZGK-UHFFFAOYSA-N 0.000 description 4
- 150000002431 hydrogen Chemical class 0.000 description 4
- 239000012263 liquid product Substances 0.000 description 4
- UOHMMEJUHBCKEE-UHFFFAOYSA-N prehnitene Chemical compound CC1=CC=C(C)C(C)=C1C UOHMMEJUHBCKEE-UHFFFAOYSA-N 0.000 description 4
- 238000004064 recycling Methods 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- 238000006276 transfer reaction Methods 0.000 description 4
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 3
- KKEYFWRCBNTPAC-UHFFFAOYSA-N Terephthalic acid Chemical compound OC(=O)C1=CC=C(C(O)=O)C=C1 KKEYFWRCBNTPAC-UHFFFAOYSA-N 0.000 description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 238000004364 calculation method Methods 0.000 description 3
- 238000004587 chromatography analysis Methods 0.000 description 3
- 238000005336 cracking Methods 0.000 description 3
- 239000003546 flue gas Substances 0.000 description 3
- 239000002808 molecular sieve Substances 0.000 description 3
- 239000001301 oxygen Substances 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- 239000012188 paraffin wax Substances 0.000 description 3
- 230000009467 reduction Effects 0.000 description 3
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 3
- YBYIRNPNPLQARY-UHFFFAOYSA-N 1H-indene Chemical compound C1=CC=C2CC=CC2=C1 YBYIRNPNPLQARY-UHFFFAOYSA-N 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 description 2
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 2
- PPBRXRYQALVLMV-UHFFFAOYSA-N Styrene Chemical compound C=CC1=CC=CC=C1 PPBRXRYQALVLMV-UHFFFAOYSA-N 0.000 description 2
- MWPLVEDNUUSJAV-UHFFFAOYSA-N anthracene Chemical compound C1=CC=CC2=CC3=CC=CC=C3C=C21 MWPLVEDNUUSJAV-UHFFFAOYSA-N 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- ZUOUZKKEUPVFJK-UHFFFAOYSA-N diphenyl Chemical compound C1=CC=CC=C1C1=CC=CC=C1 ZUOUZKKEUPVFJK-UHFFFAOYSA-N 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
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- 229910052751 metal Inorganic materials 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- YNPNZTXNASCQKK-UHFFFAOYSA-N phenanthrene Chemical compound C1=CC=C2C3=CC=CC=C3C=CC2=C1 YNPNZTXNASCQKK-UHFFFAOYSA-N 0.000 description 2
- 125000001997 phenyl group Chemical group [H]C1=C([H])C([H])=C(*)C([H])=C1[H] 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 230000008929 regeneration Effects 0.000 description 2
- 238000011069 regeneration method Methods 0.000 description 2
- 238000001179 sorption measurement Methods 0.000 description 2
- WGACMNAUEGCUHG-VYBOCCTBSA-N (2s)-2-[[(2s)-2-[[(2s)-2-acetamidopropanoyl]amino]propanoyl]amino]-n-[(2s)-6-amino-1-[[(2s)-1-[(2s)-2-[[(2s)-1-[[(2s)-5-amino-1-[[(2s)-1-[[(2s)-1-[[(2s)-6-amino-1-[[(2s)-1-amino-3-(4-hydroxyphenyl)-1-oxopropan-2-yl]amino]-1-oxohexan-2-yl]amino]-3-hydroxy- Chemical compound CC(=O)N[C@@H](C)C(=O)N[C@@H](C)C(=O)N[C@@H](CCC(N)=O)C(=O)N[C@@H](CCCCN)C(=O)N[C@@H](CCCN=C(N)N)C(=O)N1CCC[C@H]1C(=O)N[C@@H](CO)C(=O)N[C@@H](CCC(N)=O)C(=O)N[C@@H](CCCN=C(N)N)C(=O)N[C@@H](CO)C(=O)N[C@@H](CCCCN)C(=O)N[C@H](C(N)=O)CC1=CC=C(O)C=C1 WGACMNAUEGCUHG-VYBOCCTBSA-N 0.000 description 1
- 229910018072 Al 2 O 3 Inorganic materials 0.000 description 1
- CIWBSHSKHKDKBQ-JLAZNSOCSA-N Ascorbic acid Chemical compound OC[C@H](O)[C@H]1OC(=O)C(O)=C1O CIWBSHSKHKDKBQ-JLAZNSOCSA-N 0.000 description 1
- 150000001338 aliphatic hydrocarbons Chemical class 0.000 description 1
- 150000001336 alkenes Chemical class 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
- 239000011959 amorphous silica alumina Substances 0.000 description 1
- 150000001491 aromatic compounds Chemical class 0.000 description 1
- 239000011230 binding agent Substances 0.000 description 1
- 235000010290 biphenyl Nutrition 0.000 description 1
- 239000004305 biphenyl Substances 0.000 description 1
- 125000004432 carbon atom Chemical group C* 0.000 description 1
- 238000004517 catalytic hydrocracking Methods 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- RMBPEFMHABBEKP-UHFFFAOYSA-N fluorene Chemical compound C1=CC=C2C3=C[CH]C=CC3=CC2=C1 RMBPEFMHABBEKP-UHFFFAOYSA-N 0.000 description 1
- 239000011159 matrix material Substances 0.000 description 1
- 150000002739 metals Chemical class 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 108010074544 myelin peptide amide-12 Proteins 0.000 description 1
- 229910000510 noble metal Inorganic materials 0.000 description 1
- NIHNNTQXNPWCJQ-UHFFFAOYSA-N o-biphenylenemethane Natural products C1=CC=C2CC3=CC=CC=C3C2=C1 NIHNNTQXNPWCJQ-UHFFFAOYSA-N 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 125000003367 polycyclic group Chemical group 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 238000003672 processing method Methods 0.000 description 1
- 239000000377 silicon dioxide Substances 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 238000010998 test method Methods 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 238000004227 thermal cracking Methods 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
- 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
- C10G69/04—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 catalytic cracking in the absence of hydrogen
-
- 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
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The application relates to a catalytic conversion method for producing C6-C8 light aromatic hydrocarbon, which comprises the following steps: introducing raw oil into a raw material separation unit to obtain a first component rich in polycyclic aromatic hydrocarbon and a second component rich in monocyclic aromatic hydrocarbon; introducing the first component into a hydrotreating unit for hydrogenation reaction, and introducing the obtained hydrogenation component into a catalytic cracking unit; introducing a second component to the catalytic cracking unit; introducing the reaction oil gas generated by the catalytic cracking unit into a product separation unit for separation; introducing a heavy aromatic fraction to the catalytic cracking unit; and introducing the light aromatic fraction into an aromatic extraction unit for extraction to obtain C6-C8 light aromatic and raffinate oil respectively. The method can convert the raw oil into light aromatic hydrocarbon such as benzene, toluene and xylene to the maximum extent.
Description
Technical Field
The invention relates to the field of petrochemical industry, in particular to a catalytic conversion method for producing C6-C8 light aromatic hydrocarbon.
Background
In recent years, with the reduction of the demand of automotive diesel in China year by year, the reduction of the yield of the diesel and the reduction of the diesel-to-gasoline ratio are the problems which are urgently needed to be solved by refineries in the current and future time. The diesel oil related to the oil refinery mainly comprises straight-run diesel oil, catalytic cracking light cycle oil, coked diesel oil, hydrocracking diesel oil, aromatized diesel oil and the like, wherein the catalytic cracking light cycle oil is one of important products of a catalytic cracking device, and has the defects of high density, high aromatic hydrocarbon content, low cetane number and the like, so that the requirements of the diesel oil standard for vehicles are difficult to be met even through hydro-upgrading. Light aromatic hydrocarbons such as benzene, toluene and xylene are very important chemical raw materials, can be used for producing chemical products such as styrene, terephthalic acid (PTA), dimethyl terephthalate (DMT) and the like, and have the advantages of increasing the demand quantity year by year and broad market prospect. As the diesel oil contains a large amount of polycyclic aromatic hydrocarbons such as the bicyclic aromatic hydrocarbons, if the polycyclic aromatic hydrocarbons can be converted into light aromatic hydrocarbons through a reasonable processing process, the light cycle oil yield of a catalytic cracking device can be reduced, and high-value chemical raw materials can be produced.
US4585545 discloses a method for producing gasoline rich in aromatic hydrocarbons, which comprises the steps of hydrotreating a whole fraction of catalytically cracked light cycle oil, and then removing the obtained hydrogenated diesel oil for catalytic cracking to produce gasoline rich in monocyclic aromatic hydrocarbons.
CN110551526a discloses a method for processing catalytic cracking light cycle oil, which comprises the following steps: (1) Contacting the catalytic cracking light cycle oil with a hydrotreating catalyst and hydrotreating to obtain hydrogenated light cycle oil; (2) Sending the obtained hydrogenated light cycle oil and hydrogen-containing gas into a catalytic cracking reactor to contact with a catalytic cracking catalyst and perform catalytic cracking reaction to obtain a reaction product and a spent catalyst; (3) Feeding the obtained spent catalyst into a regenerator for regeneration, and feeding the obtained regenerated catalyst into a catalytic cracking reactor as the catalytic cracking catalyst; (4) And separating the obtained reaction product to obtain a dry gas product, a liquefied gas product, a gasoline product, a light cycle oil product and a heavy oil product. The processing method of the invention has the advantages of high yield of the aromatic hydrocarbon-rich gasoline, low coke generation and good raw material utilization rate.
CN103923698A discloses a catalytic conversion method for producing aromatic compounds, in the method, inferior heavy cycle oil and residual oil are subjected to hydrotreating reaction in the presence of hydrogen and hydrogenation catalyst, and reaction products are separated to obtain gas, naphtha, hydrogenated diesel oil and hydrogenated residual oil; the hydrogenated diesel oil enters a catalytic cracking device to carry out cracking reaction in the presence of a catalytic cracking catalyst, and the reaction products are separated to obtain dry gas, liquefied gas, catalytic gasoline rich in benzene, toluene and xylene, catalytic light diesel oil, distillate with the distillation range of 250-450 ℃ and slurry oil; wherein the distillate with the distillation range of 250-450 ℃ is sent to a residual oil hydrotreater for recycling. The method fully utilizes the residual oil hydrogenation condition to saturate the aromatic ring in the inferior heavy cycle oil to the greatest extent, thereby maximizing the production of benzene, toluene and xylene in the catalytic cracking of the hydrogenated diesel oil.
It can be seen that the prior art generally performs catalytic cracking after hydrotreating on diesel oil, so that the bicyclic aromatic hydrocarbon in the diesel oil can be converted into light aromatic hydrocarbon, but the yield of the light aromatic hydrocarbon in the prior art is overall low.
Disclosure of Invention
The invention aims at providing a catalytic conversion method for producing C6-C8 light aromatic hydrocarbon aiming at the defects of the prior art.
The application provides a catalytic conversion method for producing C6-C8 light aromatic hydrocarbon, which comprises the following steps:
s1, introducing raw oil into a raw material separation unit to obtain a first component rich in polycyclic aromatic hydrocarbon and a second component rich in monocyclic aromatic hydrocarbon;
s2, introducing the first component rich in the polycyclic aromatic hydrocarbon into a hydrotreating unit, carrying out hydrogenation reaction under the action of a hydrogenation catalyst, introducing the obtained hydrogenation component into a catalytic cracking unit, and contacting and reacting with a catalytic cracking catalyst in a catalytic cracking reactor of the catalytic cracking unit;
s3, introducing the second component rich in the monocyclic aromatic hydrocarbon into the catalytic cracking unit, and enabling the second component to contact with a catalytic cracking catalyst in the catalytic cracking reactor and react;
s4, introducing the reaction oil gas generated by the catalytic cracking unit into a product separation unit for separation to respectively obtain cracked gas, light aromatic fraction, heavy aromatic fraction, circulating oil fraction and heavy oil fraction;
S5, introducing the heavy aromatic fraction into the catalytic cracking unit, and enabling the heavy aromatic fraction to contact with a catalytic cracking catalyst in the catalytic cracking reactor and react;
s6, introducing the light aromatic fraction into an aromatic extraction unit for extraction to obtain C6-C8 light aromatic and raffinate oil respectively.
In one embodiment, the raffinate oil is also introduced to the catalytic cracking unit.
In one embodiment, the mixed fraction obtained after the raffinate oil is mixed with the heavy aromatic fraction, the second component rich in monocyclic aromatic hydrocarbon and the hydrogenation component are fed at different positions of the catalytic cracking reactor, and the mixed fraction feed inlet, the second component feed inlet rich in monocyclic aromatic hydrocarbon and the hydrogenation component feed inlet are sequentially arranged from bottom to top.
In one embodiment, the height of the mixed fraction feed inlet from the bottom of the catalytic cracking reactor is 0 to 1/4, preferably 0 to 1/6, of the total height of the catalytic cracking reactor; the height of the second component feed inlet rich in monocyclic aromatic hydrocarbon from the bottom of the catalytic cracking reactor accounts for 1/4 to 1/3, preferably 1/4 to 2/7 of the total height of the catalytic cracking reactor; the height of the hydrogenation component feed inlet from the bottom of the catalytic cracking reactor is 1/3-2/3, preferably 1/3-1/2 of the total height of the catalytic cracking reactor.
In one embodiment, the raffinate oil, the heavy aromatic fraction, the mixed fraction of the second component rich in monocyclic aromatic hydrocarbon and the hydrogenation component are fed at different positions of the catalytic cracking reactor, and a mixed fraction feed inlet and a hydrogenation component feed inlet are sequentially arranged from bottom to top.
In one embodiment, the height of the mixed fraction feed inlet from the bottom of the catalytic cracking reactor is 0 to 1/3, preferably 0 to 1/5, of the total height of the catalytic cracking reactor, and the height of the hydrogenation component feed inlet from the bottom of the catalytic cracking reactor is 1/3 to 2/3, preferably 1/3 to 1/2, of the total height of the catalytic cracking reactor.
In one embodiment, the amount of polycyclic aromatic hydrocarbon in the polycyclic aromatic hydrocarbon-rich first component is from 70 to 100 wt%, preferably from 80 to 100 wt%; the amount of monocyclic aromatic hydrocarbon in the second component rich in monocyclic aromatic hydrocarbon is 50 to 100% by weight, preferably 70 to 100% by weight.
In one embodiment, the raw material separation unit adopts a combination mode of one or more of distillation separation, adsorption separation, extraction separation and membrane separation.
In one embodiment, when the feedstock separation unit separates by distillation, the cut point of the first polycyclic aromatic hydrocarbon-rich component and the second monocyclic aromatic hydrocarbon-rich component is 230 to 270 ℃, preferably 240 to 260 ℃.
In one embodiment, the light aromatic fraction and the heavy aromatic fraction are cut at a point of 150 to 190 ℃, preferably 160 to 180 ℃; the cutting point of the heavy aromatic fraction and the circulating oil fraction is 200-270 ℃, preferably 230-260 ℃; the cutting point of the cycle oil fraction and the heavy oil fraction is 340 to 370 ℃, preferably 350 to 360 ℃.
In one embodiment, the content of C6-C8 aromatics in the light aromatic fraction is not less than 40 wt%, preferably not less than 50 wt%; the content of c9+ aromatic hydrocarbons in the heavy aromatic fraction is not less than 50 wt%, preferably not less than 70 wt%.
In one embodiment, the reaction temperature of the hydrotreating unit is 340-460 ℃, the hydrogen partial pressure is 5-15 MPa, and the volume space velocity is 2-15 h -1 Hydrogen oil volume ratio of 400-1600 Nm 3 /m 3 。
In one embodiment, the polycyclic aromatic hydrocarbon content of the hydrogenation component is no greater than 20 wt%, preferably no greater than 10 wt%.
In one embodiment, the reaction temperature of the catalytic cracking reactor is 520-720 ℃, preferably 560-640 ℃, the mass ratio of the catalyst to the oil is 1-50, preferably 4-20, the oil-gas residence time is 0.5-10 s, preferably 0.8-6 s, and the reaction pressure (gauge pressure) is 0-0.2 MPa, preferably 0-0.15 MPa.
In one embodiment, the aromatic hydrocarbon extraction unit has a top temperature of 70 to 100 ℃, preferably 80 to 90 ℃, a bottom temperature of 160 to 190 ℃, preferably 170 to 180 ℃, and a pressure (gauge pressure) of 0.25 to 0.6MPa, preferably 0.35 to 0.55MPa.
In one embodiment, the extraction solvent used in the aromatic hydrocarbon extraction unit is one or more of sulfolane, N-methylpyrrolidone, dimethyl sulfoxide, and formylmorpholine.
In one embodiment, the aromatic hydrocarbon extraction unit produces a C6 to C8 light aromatic hydrocarbon having a sum of benzene, toluene and xylene content of not less than 95 wt%, preferably not less than 98 wt%.
In one embodiment, the cycle oil fraction is also introduced into the hydroprocessing unit for hydrogenation; and/or the number of the groups of groups,
and introducing heavy aromatic hydrocarbon fractions generated by other devices into the catalytic cracking reactor for reaction, wherein the other devices comprise one or more of a steam cracking device, a catalytic cracking device, a hydrogenation device, a reforming device and an aromatization device.
In one embodiment, the raw oil is one or more of straight-run diesel oil, catalytic cracking light cycle oil, coker diesel oil, thermal cracking diesel oil, aromatizer diesel oil, direct coal liquefaction diesel oil and shale oil diesel oil.
The method comprises the steps of firstly separating raw oil, carrying out hydrotreatment on the obtained heavy fraction rich in polycyclic aromatic hydrocarbon, converting the heavy fraction into a hydrogenation component rich in monocyclic aromatic hydrocarbon, then carrying out contact reaction with a catalytic cracking catalyst, and directly carrying out contact reaction on the light fraction rich in monocyclic aromatic hydrocarbon with the catalytic cracking catalyst, so that the monocyclic aromatic hydrocarbon can be converted into light aromatic hydrocarbon such as benzene, toluene and xylene; the heavy aromatic fraction rich in C9+ aromatic hydrocarbon in the catalytic cracking reaction product and raffinate oil generated by an aromatic hydrocarbon extraction unit are returned to a catalytic cracking reactor for continuous reaction, and are fed in layers at different positions, so that on one hand, the C9+ aromatic hydrocarbon and the raffinate oil can be converted into light aromatic hydrocarbons such as benzene, toluene and xylene, and on the other hand, the activity of the catalyst can be reduced, and the hydrogenation component and the light fraction rich in monocyclic aromatic hydrocarbon can inhibit hydrogen transfer and condensation reaction when contacting the catalyst, so that the yield of the light aromatic hydrocarbon is improved; in addition, the circulating oil fraction rich in polycyclic aromatic hydrocarbon in the catalytic cracking product is returned to the hydrotreating unit for recycling, so that the utilization rate of the raw materials is further improved. The method returns the heavy aromatic fraction generated by catalytic cracking reaction and raffinate oil generated by aromatic extraction to the catalytic cracking reactor for secondary conversion, and returns the circulating oil fraction to the hydrotreating unit for cyclic utilization, thereby improving the yield of light aromatic hydrocarbons such as benzene, toluene, xylene and the like.
Drawings
FIG. 1 is a schematic flow chart of an embodiment of the present invention.
Fig. 2 is a schematic flow chart of another embodiment of the present invention.
Detailed Description
The present application is further described in detail below by way of the accompanying drawings and examples. The features and advantages of the present application will become more apparent from the description.
The word "exemplary" is used herein to mean "serving as an example, embodiment, or illustration. Any embodiment described herein as "exemplary" is not necessarily to be construed as preferred or advantageous over other embodiments. Although various aspects of the embodiments are illustrated in the accompanying drawings, the drawings are not necessarily drawn to scale unless specifically indicated.
The method provided by the present invention is further described below with reference to fig. 1 and 2, it being understood that the embodiments described herein are for purposes of illustration and explanation only and are not intended to limit the present invention.
In the present invention, any matters or matters not mentioned are directly applicable to those known in the art without modification except for those explicitly stated. Moreover, any embodiment described herein can be freely combined with one or more other embodiments described herein, and the technical solutions or ideas thus formed are all considered as part of the original disclosure or original description of the present invention, and should not be considered as new matters not disclosed or contemplated herein unless such combination would obviously be unreasonable to one skilled in the art.
All of the features disclosed in this invention may be combined in any combination which is understood to be disclosed or described in this invention unless the combination is obviously unreasonable by those skilled in the art. The endpoints and any values of the ranges disclosed herein are not limited to the precise range or value, and are understood to encompass values approaching those ranges or values. For numerical ranges, one or more new numerical ranges may be found between the endpoints of each range, between the endpoint of each range and the individual point value, and between the individual point value, in combination with each other, and are to be considered as specifically disclosed herein.
The application relates to a catalytic conversion method for producing C6-C8 light aromatic hydrocarbon, which comprises the following steps:
s1, introducing raw oil into a raw material separation unit to obtain a first component rich in polycyclic aromatic hydrocarbon and a second component rich in monocyclic aromatic hydrocarbon;
s2, introducing the first component rich in the polycyclic aromatic hydrocarbon into a hydrotreating unit, carrying out hydrogenation reaction under the action of a hydrogenation catalyst, introducing the obtained hydrogenation component into a catalytic cracking unit, and contacting and reacting with the catalytic cracking catalyst in a catalytic cracking reactor;
S3, introducing the second component rich in the monocyclic aromatic hydrocarbon into a catalytic cracking unit, and enabling the second component to contact with a catalytic cracking catalyst in a catalytic cracking reactor and react;
s4, introducing the reaction oil gas generated by the catalytic cracking unit into a product separation unit for separation to respectively obtain cracked gas, light aromatic fraction, heavy aromatic fraction, circulating oil fraction and heavy oil fraction;
s5, introducing the heavy aromatic fraction into the catalytic cracking unit, and enabling the heavy aromatic fraction to contact with a catalytic cracking catalyst in a catalytic cracking reactor and react;
s6, introducing the light aromatic fraction into an aromatic extraction unit for extraction to obtain C6-C8 light aromatic and raffinate oil respectively.
The method of the present application is further described below in conjunction with fig. 1 and 2.
In this application, light aromatic hydrocarbon refers to C6-C8 aromatic hydrocarbon including benzene, toluene, xylene, etc. "polycyclic aromatic hydrocarbon" refers to aromatic hydrocarbons containing two or more benzene rings, and includes non-condensed ring type aromatic hydrocarbons such as biphenyl, and polycyclic substituted aliphatic hydrocarbons, and condensed ring type aromatic hydrocarbons such as naphthalene, anthracene, phenanthrene, indene, fluorene, acenaphthene, hydrocarbon derivatives thereof, and the like. "monocyclic aromatic hydrocarbon" means an aromatic hydrocarbon containing one benzene ring, such as benzene, toluene, xylene, trimethylbenzene, tetramethylbenzene, and the like. "C9+ aromatic hydrocarbon" means an aromatic hydrocarbon having 9 or more carbon atoms, such as trimethylbenzene, tetramethylbenzene, etc.
The process provided by the present invention can be carried out by a production apparatus as described in fig. 1 and 2, which comprises at least a feedstock separation unit 1, a hydrotreating unit 2, a catalytic cracking unit 3, a product separation unit 4 and an aromatic hydrocarbon extraction unit 5.
In the present invention, the feedstock separation unit 1 is used to separate the feedstock 101 into a first component 102 rich in polycyclic aromatic hydrocarbons and a second component 103 rich in monocyclic aromatic hydrocarbons. The raw oil 101 used in the present invention may be one or more of straight-run diesel, catalytically cracked light cycle oil, coker diesel, hydrocracker diesel, reformed diesel, and aromatizer diesel.
By separating the raw oil 101 into two components by the raw material separation unit 1, the second component 103 rich in monocyclic aromatic hydrocarbon can directly enter the catalytic cracking unit 3 for catalytic cracking, and the first component 102 rich in polycyclic aromatic hydrocarbon can enter the hydrotreating unit 2 for hydrotreating, whereby the load of the hydrotreating unit can be reduced.
In one embodiment, the amount of polycyclic aromatic hydrocarbon in the polycyclic aromatic hydrocarbon-rich first component 102 is from 70 to 100 percent by weight, preferably from 80 to 100 percent by weight, based on the total weight of the polycyclic aromatic hydrocarbon-rich first component. The amount of monocyclic aromatic hydrocarbon in the second component 103 rich in monocyclic aromatic hydrocarbon is 50 to 100% by weight, preferably 70 to 100% by weight, based on the total weight of the second component rich in monocyclic aromatic hydrocarbon.
The method of separation in the raw material separation unit 1 may include various methods such as one or more of distillation separation, adsorption separation, extraction separation, membrane separation, and the like. Preferably, the raw material separation unit 1 is preferably flash separation, and the temperature of the flash separation is 230-270 ℃, preferably 240-260 ℃, and the pressure (gauge pressure) is 0-0.4 MPa, preferably 0.05-0.25 MPa. Thus, the cut point of the second component 103 rich in monocyclic aromatic hydrocarbon and the first component 102 rich in polycyclic aromatic hydrocarbon is 230 to 270 ℃, preferably 240 to 260 ℃. By this flash separation, the fraction having a distillation range higher than the cut point is the first component 102 rich in polycyclic aromatic hydrocarbons, and the fraction having a distillation range lower than the cut point is the second component 103 rich in monocyclic aromatic hydrocarbons.
In the present invention, the hydrotreating unit 2 is used to hydrotreat the material in the hydrotreating unit 2 to convert the material into a hydrogenation component 204 rich in monocyclic aromatic hydrocarbon. As shown in fig. 1 and 2, the feed to hydroprocessing unit 2 may include a first component 102 rich in polyaromatic hydrocarbons from feed separation unit 1 and a cycle oil fraction 409 from product separation unit 4, which cycle oil fraction 409 from product separation unit 4 may be recycled back to hydroprocessing unit 2, improving the yield of light aromatic hydrocarbons as a product.
The hydroprocessing unit 2 comprises a hydrogenation reactor, which may be a fixed bed reactor. To increase the throughput of the hydroprocessing unit, multiple hydrogenation reactors may be used in series or parallel arrangements. The reaction temperature of the hydrotreating unit 2 can be 340-460 ℃, the hydrogen partial pressure is 5-15 MPa, and the volume airspeed is 2-15 h -1 Hydrogen oil volume ratio of 400-1600 Nm 3 /m 3 . The hydrogenation catalyst comprises an active component and a carrier, wherein the active component is selected from a group VIB metal, a group VIII non-noble metal or a mixture of two metals, and the carrier is selected from one or a mixture of more of alumina, silica and amorphous silica-alumina. The content of polycyclic aromatic hydrocarbon in the hydrotreated component 204 obtained after the hydrotreatment is not more than 20% by weight, preferably not more than 10% by weight.
In the present invention, the catalytic cracking unit 3 includes a catalytic cracking reactor and a regenerator (not shown in the figure), the hydrogenation component 204 and the second component 103 rich in monocyclic aromatic hydrocarbon contact react with the catalytic cracking catalyst in the catalytic cracking reactor, the generated oil mixture is separated by a separation device, the generated reaction oil gas 305 is introduced into the product separation unit 4, the spent catalyst is introduced into the regenerator for regeneration after being stripped, and the regenerated catalytic cracking catalyst is returned to the reactor for recycling.
The catalytic cracking reactor of the catalytic cracking unit 3 may use various reactors commonly used in the art, and may be selected from, for example, one or more types of combination of fixed bed reactors, moving bed reactors, fluidized bed reactors, riser reactors, preferably riser reactors selected from one of equal-diameter riser reactors and variable-diameter riser reactors.
In this application, the heavy aromatic fraction 408 from the product separation unit 4 is also introduced into the catalytic cracking unit 3 where it contacts and reacts with the catalytic cracking catalyst. The heavy aromatics fraction 408 contains c9+ aromatics, which are recycled directly back to the catalytic cracking reactor of catalytic cracking unit 3 for catalytic cracking reactions. The present application specifically distinguishes the products separated by the product separation unit 4, and respectively obtains a light aromatic fraction 407, a heavy aromatic fraction 408 and a circulating oil fraction 409, and adopts different treatment modes for the three different fractions: the light aromatic fraction 407 is directly subjected to extraction treatment to obtain a target product C6-C8 light aromatic; the heavy aromatic fraction 408 is directly recycled to the catalytic cracking unit 3 for catalytic cracking reaction; while the cycle oil fraction 409 is recycled back to the hydroprocessing unit 2 for hydroprocessing. The treatment mode can not only improve the yield of target products C6-C8 light aromatic hydrocarbon, but also reduce the load of a hydrotreating unit, reduce the hydrogen consumption and the like.
In one embodiment, the raffinate oil 512 is also introduced into the catalytic cracking unit 3 for catalytic cracking reactions. In one embodiment, the raffinate oil 512 and the mixed fraction of the heavy aromatic fraction 408 are introduced together into the catalytic cracking unit 3 to perform a catalytic cracking reaction.
For this purpose, the catalytic cracking reactor may be provided with a plurality of feed inlets. As shown in fig. 1, in one embodiment, the catalytic cracking reactor may be provided with a mixed fraction feed port 301, a second component feed port 302, and a hydrogenation component feed port 303, which are provided at different positions of the catalytic cracking reactor, in order from bottom to top, the mixed fraction feed port 301, the second component feed port 302, and the hydrogenation component feed port 303. As shown in fig. 1, a mixed fraction feed port 301 is used to feed the mixed fraction 13 of the raffinate 512 and the heavy aromatic fraction 408, a second component feed port 302 is used to feed the second component 103 enriched in monocyclic aromatic hydrocarbons from the feedstock separation unit 1, and a hydrogenation component feed port 303 is used to feed the hydrogenation component 204 from the hydrotreating unit 2. In one embodiment, the height of the mixed fraction feed inlet 301 from the bottom of the catalytic cracking reactor is 0 to 1/4, preferably 0 to 1/6 of the total height of the catalytic cracking reactor; the height of the second component feed inlet 302 from the bottom of the catalytic cracking reactor is 1/4 to 1/3, preferably 1/4 to 2/7 of the total height of the catalytic cracking reactor; the height of the hydrogenation component feed inlet 303 from the bottom of the catalytic cracking reactor is 1/3 to 2/3, preferably 1/3 to 1/2, of the total height of the catalytic cracking reactor. By adopting the feeding mode, the mixed fraction of the raffinate oil 512 and the heavy aromatic fraction 408 and the second component 103 rich in the monocyclic aromatic hydrocarbon can be respectively contacted with the high-temperature regenerated catalyst in sequence, so that a small amount of carbon deposit is generated on the regenerated catalyst, the activity of the regenerated catalyst is reduced, the occurrence of hydrogen transfer and condensation reaction is inhibited when the hydrogenation component 204 is contacted with the catalyst, the hydrogenation component 204 is favorably converted into C6-C8 light aromatic hydrocarbon more, and the yield of the C6-C8 light aromatic hydrocarbon is improved.
As shown in fig. 2, in one embodiment, the catalytic cracking reactor may be provided with a mixed fraction feed port 301 and a hydrogenation component feed port 303, which are provided at different positions of the catalytic cracking reactor, and the mixed fraction feed port 301 and the hydrogenation component feed port 303 are sequentially provided from bottom to top. As shown in fig. 2, the mixed fraction feed port 301 is used to feed the raffinate 512, the mixed fraction 13 of the second component 103 enriched in monocyclic aromatic hydrocarbons and the heavy aromatic hydrocarbon fraction 408, and the hydrogenation component feed port 303 is used to feed the hydrogenation component 204 from the hydrotreating unit 2. In one embodiment, the height of the mixed fraction feed inlet 301 from the bottom of the catalytic cracking reactor is 0 to 1/3, preferably 0 to 1/5, of the total height of the catalytic cracking reactor, and the height of the hydrogenation component feed inlet 303 from the bottom of the catalytic cracking reactor is 1/3 to 2/3, preferably 1/3 to 1/2, of the total height of the catalytic cracking reactor. Likewise, by adopting the feeding mode, the raffinate oil 512, the second component 103 rich in the monocyclic aromatic hydrocarbon and the mixed fraction of the heavy aromatic hydrocarbon fraction 408 can be firstly contacted with the high-temperature regenerated catalyst, so that a small amount of carbon deposit is generated on the regenerated catalyst, the activity of the regenerated catalyst is reduced, the occurrence of hydrogen transfer and condensation reaction is inhibited when the subsequent hydrogenation component 204 is contacted with the catalyst, the hydrogenation component 204 is more converted into C6-C8 light aromatic hydrocarbon, and the yield of the C6-C8 light aromatic hydrocarbon is improved.
In addition, in one embodiment, the heavy aromatic fraction produced by other devices may be introduced into the catalytic cracking reactor of the catalytic cracking unit 3 to perform a reaction, including one or more of a steam cracker, a catalytic cracker, a hydrogenation device, a reformer, and an aromatizer.
The reaction temperature of the catalytic cracking reactor in the catalytic cracking unit 3 is 520-720 ℃, preferably 560-640 ℃, the mass ratio of catalyst to oil is 1-50, preferably 4-20, the oil-gas residence time is 0.5-10 s, preferably 0.8-6 s, and the reaction pressure (gauge pressure) is 0-0.2 MPa, preferably 0-0.15 MPa. The catalytic cracking catalyst comprises 15-60 wt% of cracking active components, 15-90 wt% of matrix and 0-20 wt% of binder, wherein the cracking active components are selected from one or a mixture of a plurality of unmodified, phosphorus-modified, rare earth-modified or phosphorus-and-rare earth-modified Y molecular sieves, beta molecular sieves and ZSM-5 molecular sieves. The catalytic cracking catalyst has an activity of not less than 65, preferably not less than 68.
In the present invention, the product separation unit 4 is used to separate the reaction oil gas 305 from the catalytic cracking unit 3 into various products. The product separation unit 4 generally adopts rectification separation, and can be in the forms of a plate tower, a floating valve tower, a packing tower and the like, and the separation requirement is met by setting reasonable theoretical plate numbers and tower diameters. The reaction oil gas 305 generated by the catalytic cracking unit 3 can be separated into a cracked gas 406, a light aromatic fraction 407, a heavy aromatic fraction 408, a cycle oil fraction 409, and a heavy oil fraction 410 by the product separation unit 4. The light aromatic fraction 407 and the heavy aromatic fraction 408 have a cut point of 150 to 190 ℃, preferably 160 to 180 ℃. The cutting point of the heavy aromatic fraction 408 and the cycle oil fraction 409 is 200 to 270 ℃, preferably 230 to 260 ℃. The cutting point of the cycle oil fraction 409 and the heavy oil fraction 410 is 340 to 370 ℃, preferably 350 to 360 ℃.
In one embodiment, the content of C6-C8 aromatics in the light aromatic fraction 407 is not less than 40 wt%, preferably not less than 50 wt%. The content of c9+ aromatics in the heavy aromatics fraction 408 is not less than 50 wt%, preferably not less than 70 wt%. As described above, the heavy aromatic fraction 408 is introduced into the catalytic cracking unit 3 to continue the reaction, and the cycle oil fraction 409 is introduced into the hydrotreating unit 2 to perform the hydrogenation reaction.
In the present invention, the aromatic hydrocarbon extraction unit 5 is used for C6 to C8 aromatic hydrocarbons in the light aromatic hydrocarbon fraction 407. The aromatic hydrocarbon extraction unit 5 may employ an extraction column having a column top temperature of 70 to 100 ℃, preferably 80 to 90 ℃, a column bottom temperature of 160 to 190 ℃, preferably 170 to 180 ℃, and a pressure (gauge pressure) of 0.25 to 0.6MPa, preferably 0.35 to 0.55MPa. The extraction solvent used in the aromatic hydrocarbon extraction unit 5 may be one or more of sulfolane, N-methylpyrrolidone, dimethyl sulfoxide and formyl morpholine. The sum of benzene, toluene and xylene content in the C6-C8 aromatic 511 obtained by the aromatic extraction unit 5 is not less than 95% by weight, preferably not less than 98% by weight. As previously described, the resulting raffinate 512 may be introduced into the catalytic cracking unit 3 to continue the catalytic cracking reaction.
In one embodiment of the invention, the raw oil 101 is preheated to 230-270 ℃ and then introduced into a raw material separation unit 1, and is separated into a first component 102 rich in polycyclic aromatic hydrocarbon and a second component 103 rich in monocyclic aromatic hydrocarbon in the raw material separation unit, wherein the raw material separation unit 1 adopts a flash separation mode, and the cutting point of the first component 102 rich in polycyclic aromatic hydrocarbon and the second component 103 rich in monocyclic aromatic hydrocarbon is 230-270 ℃, preferably 240-260 ℃. The first component 102 rich in polycyclic aromatic hydrocarbon is sprayed into a hydrogenation reactor of a hydrotreating unit 2 through a nozzle, and is reacted with a hydrogenation catalyst at a reaction temperature of 340-460 ℃, a hydrogen partial pressure of 5-15 MPa and a volume space velocity of 2-15 h -1 Hydrogen oil volume ratio of 400-1600 Nm 3 /m 3 The obtained hydrogenation component 204 is introduced into a hydrogenation component feed inlet 303 of a catalytic cracking reactor in a catalytic cracking unit 3, sprayed into the catalytic cracking reactor through a nozzle, and is contacted and reacted with the catalytic cracking catalyst at a reaction temperature of 520-720 ℃, preferably 560-640 ℃, the catalyst-to-oil mass ratio of 1-50, preferably 4-20, the oil-gas residence time of 0.5-10 s, preferably 0.8-6 s, the reaction pressure (gauge pressure) of 0-0.2 MPa, preferably 0-0.15 MPa, the second component 103 rich in monocyclic aromatic hydrocarbon obtained in the raw material separation unit 1 is introduced into a second component feed inlet 302 of the catalytic cracking reactor in the catalytic cracking unit 3, sprayed into the catalytic cracking reactor through a nozzle, contacted and reacted with the catalytic cracking catalyst, and the generated reaction oil gas 305 is introduced into a product separation unit 4 for separation, thereby obtaining a cracked gas 406, a light aromatic hydrocarbon fraction 407, a heavy aromatic hydrocarbon fraction 408, a circulating oil 409 and a heavy oil fraction 410 respectively. Wherein, the light aromatic fraction 407 is introduced into an aromatic extraction unit 5, and is extracted in an extraction tower under the conditions that the temperature of the top of the tower is 70-100 ℃, preferably 80-90 ℃, the temperature of the bottom of the tower is 160-190 ℃, preferably 170-180 ℃, and the pressure (gauge pressure) is 0.25-0.6 MPa, preferably 0.35-0.55 MPa, wherein the extraction solvent is one or more of sulfolane, N-methylpyrrolidone, dimethyl sulfoxide and formylmorpholine, and the sum of the contents of benzene, toluene and xylene is not less than 95 percent, preferably not less than 98 percent of C6-C8 aromatic hydrocarbon 511 and raffinate 512 by weight; the mixed fraction 13 obtained by mixing the raffinate oil 512 with the heavy aromatic fraction 408 is returned to the mixed fraction feed inlet 301 on the catalytic cracking reactor, is sprayed into the catalytic cracking reactor through a nozzle, and is contacted and reacted with the catalytic cracking catalyst from the bottom of the catalytic cracking reactor. The mixed fraction 13 obtained by mixing the raffinate 512 with the heavy aromatic fraction 408, the second component 103 and the hydrogenation component 204 are fed at different positions of the catalytic cracking reactor, and a mixed fraction feed inlet 301, a second component feed inlet 302 and a hydrogenation component feed inlet 303 are sequentially arranged from bottom to top. The height of the mixed fraction feed inlet 301 from the bottom of the catalytic cracking reactor is 0 to 1/4, preferably 0 to 1/6, of the total height of the catalytic cracking reactor, and the second component feed inlet 302 is spaced from the catalytic cracking reactor The height of the bottom of the reactor is 1/4 to 1/3, preferably 1/4 to 2/7 of the total height of the catalytic cracking reactor, and the height of the hydrogenation component feed inlet 303 from the bottom of the catalytic cracking reactor is 1/3 to 2/3, preferably 1/3 to 1/2 of the total height of the catalytic cracking reactor. The cycle oil fraction 409 is introduced into the hydrotreating unit 2 for hydrogenation.
In another embodiment of the present invention, the raffinate oil 512, the heavy aromatic fraction 408 and the second component 103 rich in monocyclic aromatic are mixed to obtain a mixed fraction 13 and the hydrogenation component 204, which are fed at different positions of the catalytic cracking reactor, and the mixed fraction feed inlet 301 and the hydrogenation component feed inlet 303 are sequentially arranged from bottom to top. The height of the mixed fraction feed inlet 301 from the bottom of the catalytic cracking reactor is 0 to 1/3, preferably 0 to 1/5, of the total height of the catalytic cracking reactor, and the height of the hydrogenation component feed inlet 303 from the bottom of the catalytic cracking reactor is 1/3 to 2/3, preferably 1/3 to 1/2, of the total height of the catalytic cracking reactor.
The method comprises the steps of firstly separating raw oil, particularly catalytic cracking light cycle oil, carrying out hydrotreatment on the obtained heavy fraction rich in polycyclic aromatic hydrocarbon, converting the heavy fraction into a hydrogenation component rich in monocyclic aromatic hydrocarbon, then carrying out contact reaction with a catalytic cracking catalyst, and directly carrying out contact reaction on the light fraction rich in monocyclic aromatic hydrocarbon with the catalytic cracking catalyst, so that the monocyclic aromatic hydrocarbon can be converted into light aromatic hydrocarbon such as benzene, toluene, xylene and the like; the heavy aromatic fraction rich in C9+ aromatic hydrocarbon in the catalytic cracking reaction product and raffinate oil generated by an aromatic hydrocarbon extraction unit are returned to a catalytic cracking reactor for continuous reaction, and are fed in layers at different positions, so that on one hand, the C9+ aromatic hydrocarbon and the raffinate oil can be converted into light aromatic hydrocarbons such as benzene, toluene and xylene, and on the other hand, the activity of the catalyst can be reduced, and the hydrogenation component and the light fraction rich in monocyclic aromatic hydrocarbon can inhibit hydrogen transfer and condensation reaction when contacting the catalyst, thereby improving the yield of the light aromatic hydrocarbon; in addition, the circulating oil fraction rich in the aromatic hydrocarbon with more than double rings in the catalytic cracking product is returned to the hydrotreating unit for recycling, so that the utilization rate of raw materials is further improved.
The present invention will be described in detail with reference to examples, but the scope of the present invention is not limited thereto.
Reagents, instruments and tests
In the examples and comparative examples of the present invention, the gas product was tested by the petrochemical analysis method RIPP 77-90, the coke content was measured by the petrochemical analysis method RIPP 107-90, and the composition of the organic liquid product was measured by the SH/T0558-1993 method.
In the examples below, the yield of the product was calculated according to the following formula:
the RIPP petrochemical analysis method used in the present invention is selected from the group consisting of "petrochemical analysis method (RIPP test method)", code Yang Cuiding, scientific Press, 1990.
The hydrogenation catalyst used in the hydrogenation unit comprises a hydrogenation catalyst RN-32V and a hydrogenation protection catalyst RG-1, wherein both catalysts are commercial catalysts and are produced by Qilu division of China petrochemical catalyst company. The catalytic cracking catalyst used in the catalytic cracking unit was produced by ziluta corporation, a petrochemical catalyst company, with a trade designation SLA-1, and its composition and properties are shown in table 1. The extraction solvent used in the aromatic hydrocarbon extraction unit is sulfolane.
TABLE 1 composition and Properties of SLA-1 catalyst
| Catalyst | SLA-1 |
| Chemical composition,% (w) | |
| Al 2 O 3 | 51.50 |
| Na 2 O | 0.15 |
| Specific surface area/(m) 2 ·g -1 ) | 125.0 |
| Pore volume/(cm) 3 ·g -1 ) | 0.3 |
| Particle size distribution,% (w) | |
| 0-20μm | 2.6 |
| 0-40μm | 21.7 |
| 0-80μm | 67.2 |
| 0-105μm | 84.1 |
| ＞105μm | 15.9 |
| Micro-inverse Activity,% (w) | 76 |
TABLE 2 Properties of catalytically cracked light cycle oil
| Project | Catalytic cracking light cycle oil |
| Density (20 ℃ C.)/(kg/m) 3 ) | 996.9 |
| Mass group composition/% | |
| Paraffin hydrocarbons | 1.2 |
| Cycloalkane (CNS) | 0.3 |
| Aromatic hydrocarbons | 98.5 |
| Monocyclic aromatic hydrocarbon | 14.4 |
| Distillation range/. Degree.C | |
| Initial point of distillation | 200 |
| 10％ | 233 |
| 30％ | 246 |
| 50％ | 255 |
| 70％ | 266 |
| 90％ | 299 |
| End point of distillation | 343 |
TABLE 3 composition and Properties of hydrogenation Components
| Project | Hydrogenation component |
| Density (20 ℃ C.)/(kg/m) 3 ) | 910.4 |
| Mass group composition/% | |
| Paraffin hydrocarbons | 12.5 |
| Cycloalkane (CNS) | 19.6 |
| Aromatic hydrocarbons | 67.9 |
| Monocyclic aromatic hydrocarbon | 56.4 |
| Distillation range/. Degree.C | |
| Initial point of distillation | 155 |
| 10％ | 202 |
| 30％ | 226 |
| 50％ | 242 |
| 70％ | 261 |
| 90％ | 300 |
| End point of distillation | 336 |
TABLE 4 composition and Properties of heavy aromatic fractions
| Project | Heavy aromatic fraction |
| Density (20 ℃ C.)/(kg/m) 3 ) | 868.4 |
| Mass group composition/% | |
| Paraffin hydrocarbons | 14.60 |
| Cycloalkane (CNS) | 0.04 |
| Olefins | 0.59 |
| Aromatic hydrocarbons | 84.77 |
| Totals to | 100 |
| Distillation range/. Degree.C | |
| Initial point of distillation | 161 |
| 10％ | 165 |
| 30％ | 167 |
| 50％ | 172 |
| 70％ | 173 |
| 90％ | 179 |
| End point of distillation | 185 |
Example 1
The preheated catalytic cracking light cycle oil is introduced into a raw material separation unit to obtain a first component and a second component, wherein the first component is hydrotreated to obtain a hydrogenated component and the second component are both introduced into a small fixed fluidized bed reactor, in addition, heavy aromatic fraction separated by a product separation unit is introduced into the small fixed fluidized bed reactor, the heavy aromatic fraction, the second component and the hydrogenated first component are sequentially and respectively fed into the three raw materials from bottom to top through feed inlets, the height of the heavy aromatic fraction feed inlet from the bottom of the catalytic cracking reactor is 1/6 of the total height of the catalytic cracking reactor, the height of the second component feed inlet from the bottom of the catalytic cracking reactor is 1/4 of the total height of the catalytic cracking reactor, and the height of the hydrogenated component feed inlet from the bottom of the catalytic cracking reactor is 1/3 of the total height of the catalytic cracking reactor. All raw materials are contacted with SLA-1 catalyst in a reactor and react, the generated oil solution mixture is separated by a filter, the separated oil gas is introduced into a product separation unit, the obtained cracked gas is analyzed for composition by gas chromatography, liquid products (light aromatic hydrocarbon fraction, heavy aromatic hydrocarbon fraction, circulating oil fraction and heavy oil fraction) are collected and analyzed for distillation range and hydrocarbon composition by gas chromatography, wherein the heavy aromatic hydrocarbon fraction is circulated back to the fluidized bed reactor, and the light aromatic hydrocarbon fraction is extracted by using sulfolane as an extraction solvent to obtain light aromatic hydrocarbon components. The catalyst after the reaction is regenerated by oxygen, and CO in the regenerated flue gas is analyzed by chromatography 2 To calculate the yield of coke. The yields of the respective products were obtained by calculation. The properties of the feedstock oil used in the examples, the light cycle oil for catalytic cracking, the hydrogenation component obtained in the hydrotreating unit and the heavy aromatic fraction obtained in the product separation unit are shown in tables 2, 3 and 4, respectively. The reaction conditions and results are shown in Table 5.
Example 2
The procedure of example 1 was followed except that the reaction temperature of the catalytic cracking reactor was changed to 610 ℃. The reaction conditions and results are shown in Table 5.
Comparative example 1
Introducing preheated catalytic cracking light cycle oil into a raw material separation unit to obtain a first component and a second component, introducing the hydrogenated component obtained after the first component is hydrogenated into a small fixed fluidized bed reactor, contacting with an SLA-1 catalyst in the reactor and reacting, separating the produced oil-gas mixture through a filter, introducing separated oil gas into a product separation unit, analyzing the composition of the obtained cracked gas through gas chromatography, collecting liquid products (light aromatic hydrocarbon fraction, heavy aromatic hydrocarbon fraction, cycle oil fraction and heavy oil fraction), analyzing the distillation range and hydrocarbon composition through gas chromatography, and extracting the obtained light aromatic hydrocarbon fraction by using sulfolane as an extraction solvent to obtain the light aromatic hydrocarbon component. The catalyst after the reaction is regenerated by oxygen, and CO in the regenerated flue gas is analyzed by chromatography 2 To calculate the yield of coke. The yields of the respective products were obtained by calculation. The reaction conditions and results are shown in Table 5.
Comparative example 2
The preheated catalytic cracking light cycle oil is introduced into a small fixed fluidized bed reactor, in addition, the separated heavy aromatic fraction is introduced into the small fixed fluidized bed reactor, the heavy aromatic fraction and the catalytic cracking light cycle oil are respectively fed into the feed inlets of the two raw materials from bottom to top in sequence, the height of the feed inlet of the heavy aromatic fraction from the bottom of the catalytic cracking reactor is 1/6 of the total height of the catalytic cracking reactor, and the height of the feed inlet of the catalytic cracking light cycle oil from the bottom of the catalytic cracking reactor is 1/4 of the total height of the catalytic cracking reactor. All ofThe raw materials are contacted with SLA-1 catalyst in a reactor and react, the generated oil mixture is separated by a filter, the separated oil gas is introduced into a product separation unit, the obtained cracked gas is analyzed for composition by gas chromatography, liquid products (light aromatic hydrocarbon fraction, heavy aromatic hydrocarbon fraction, circulating oil fraction and heavy oil fraction) are collected and analyzed for distillation range and hydrocarbon composition by gas chromatography, and the obtained light aromatic hydrocarbon fraction is extracted by using sulfolane as an extraction solvent to obtain a light aromatic hydrocarbon component. The catalyst after the reaction is regenerated by oxygen, and CO in the regenerated flue gas is analyzed by chromatography 2 To calculate the yield of coke. The yields of the respective products were obtained by calculation. The reaction conditions and results are shown in Table 5.
TABLE 5 reaction conditions and results for examples 1-2 and comparative examples 1-2
| Project | Example 1 | Example 2 | Comparative example 1 | Comparative example 2 |
| Raw material separation unit | ||||
| Temperature/. Degree.C | 250 | 250 | 250 | |
| pressure/MPa | 0.13 | 0.13 | 0.13 | |
| Hydrotreatment unit | ||||
| Reaction temperature/. Degree.C | 430 | 430 | 430 | |
| Hydrogen partial pressure/MPa | 12 | 12 | 12 | |
| Volume space velocity/h -1 | 12 | 12 | 12 | |
| Hydrogen oil volume ratio/(Nm) 3 /m 3 ) | 1300 | 1300 | 1300 | |
| Catalytic cracking unit | ||||
| Reaction temperature/. Degree.C | 630 | 610 | 630 | 610 |
| Mass ratio of agent to oil | 8 | 8 | 8 | 8 |
| Residence time/s | 5 | 5 | 5 | 5 |
| Reaction pressure/MPa | 0.12 | 0.12 | 0.12 | 0.12 |
| Product separation unit | ||||
| Cutting point/. Degree.C | ||||
| Light aromatic fraction and heavy aromatic fraction | 175 | 175 | 175 | 175 |
| Heavy aromatic fraction and cycle oil fraction | 250 | 250 | 250 | 250 |
| Cycle oil fraction and heavy oil fraction | 345 | 345 | 345 | 345 |
| Light aromatic yield/wt% | ||||
| Benzene | 3.82 | 3.61 | 2.35 | 2.19 |
| Toluene (toluene) | 13.27 | 12.96 | 8.09 | 8.40 |
| Xylene (P) | 11.87 | 11.18 | 6.55 | 8.60 |
| Sum of light aromatic hydrocarbons | 28.96 | 27.75 | 16.99 | 19.18 |
Example 3
Introducing preheated catalytic cracking light cycle oil into a flash tank for separation to respectively obtain a first component rich in polycyclic aromatic hydrocarbon and a second component rich in monocyclic aromatic hydrocarbon, wherein the first component rich in polycyclic aromatic hydrocarbon is introduced into a fixed bed hydrogenation reactor, contacts with a mixed catalyst of a hydrotreating catalyst RN-32V and a hydrogenation protecting catalyst RG-1 and carries out hydrogenation reaction, and the obtained hydrogenation component is introduced into a hydrogenation component feed inlet of the catalytic cracking reactor and reacts with an SLA-1 catalyst from the bottom of the catalytic cracking reactor in a contact way; introducing a second component rich in monocyclic aromatic hydrocarbon into a light fraction feed inlet of a catalytic cracking reactor, and carrying out contact reaction with an SLA-1 catalyst from the bottom of the catalytic cracking reactor; the produced reaction oil gas is introduced into a product separation unit for separation to respectively obtain cracked gas, light aromatic hydrocarbon fraction, heavy aromatic hydrocarbon fraction, circulating oil fraction and heavy oil fraction, wherein the light aromatic hydrocarbon fraction is introduced into an aromatic hydrocarbon extraction tower, sulfolane is used as an extraction solvent for extraction to obtain C6-C8 aromatic hydrocarbon rich in benzene, toluene and xylene and raffinate oil, the raffinate oil and the heavy aromatic hydrocarbon fraction are mixed and returned to a mixed fraction feed inlet of a catalytic cracking reactor for contact reaction with a catalytic cracking catalyst from the bottom of the catalytic cracking reactor, and the circulating oil fraction is mixed with a first component rich in polycyclic aromatic hydrocarbon and then introduced into a hydrogenation reactor for hydrogenation reaction. Wherein the height of the mixed fraction feed inlet from the bottom of the catalytic cracking reactor is 1/8 of the total height of the catalytic cracking reactor, the height of the light fraction feed inlet from the bottom of the catalytic cracking reactor is 1/4 of the total height of the catalytic cracking reactor, and the height of the hydrogenation component feed inlet from the bottom of the catalytic cracking reactor is 1/3 of the total height of the catalytic cracking reactor. The conditions and product yields for each treatment unit are shown in table 6.
Example 4
The process according to example 3 is different in that the raffinate oil, the heavy aromatic fraction and the second component rich in monocyclic aromatic are mixed and then introduced into the mixed fraction feed inlet of the catalytic cracking reactor, the hydrogenation component is introduced into the hydrogenation component feed inlet of the catalytic cracking reactor, the height of the mixed fraction feed inlet from the bottom of the catalytic cracking reactor is 1/4 of the total height of the catalytic cracking reactor, and the height of the hydrogenation component feed inlet from the bottom of the catalytic cracking reactor is 1/3 of the total height of the catalytic cracking reactor. The conditions and product yields for each treatment unit are shown in table 6.
Comparative example 3
The procedure of example 3 was followed, except that the heavy aromatic fraction obtained in the product separation unit and the raffinate oil obtained in the aromatic extraction unit were not returned to the catalytic cracking reactor for further reaction. The conditions and product yields for each treatment unit are shown in table 6.
Comparative example 4
The procedure of example 3 was followed, except that the heavy aromatic fraction obtained in the product separation unit and the raffinate oil obtained in the aromatic extraction unit were not returned to the catalytic cracking reactor to continue the reaction, and the cycle oil fraction obtained in the product separation unit was not introduced into the hydrotreating reactor to carry out the hydrogenation reaction. The conditions and product yields for each treatment unit are shown in table 6.
As can be seen from tables 5 and 6, the method and apparatus of the present invention can improve the yield of light aromatic hydrocarbon as compared with the comparative examples.
The present application has been described in connection with the preferred embodiments, but these embodiments are merely exemplary and serve only as illustrations. On the basis of this, many alternatives and improvements can be made to the present application, which fall within the scope of protection of the present application.
TABLE 6 reaction conditions and results for examples 3-4 and comparative examples 3-4
| Project | Example 3 | Example 4 | Comparative example 3 | Comparative example 4 |
| Raw material separation unit | ||||
| Temperature/. Degree.C | 250 | 260 | 250 | 260 |
| pressure/MPa | 0.12 | 0.25 | 0.15 | 0.25 |
| Hydrotreatment unit | ||||
| Reaction temperature/. Degree.C | 390 | 430 | 390 | 430 |
| Hydrogen partial pressure/MPa | 10 | 12 | 10 | 12 |
| Volume space velocity/h -1 | 8 | 12 | 8 | 12 |
| Hydrogen oil volume ratio/(Nm) 3 /m 3 ) | 800 | 1300 | 800 | 1300 |
| Catalytic cracking unit | ||||
| Reaction temperature/. Degree.C | 600 | 630 | 600 | 630 |
| Mass ratio of agent to oil | 8 | 14 | 8 | 14 |
| Residence time/s | 5 | 7 | 5 | 7 |
| Reaction pressure/MPa | 0.1 | 0.12 | 0.1 | 0.12 |
| Product separation unit | ||||
| Cutting point/. Degree.C | ||||
| Light aromatic fraction and heavy aromatic fraction | 175 | 185 | 175 | 185 |
| Heavy aromatic fraction and cycle oil fraction | 250 | 260 | 250 | 260 |
| Cycle oil fraction and heavy oil fraction | 345 | 355 | 345 | 355 |
| Aromatic hydrocarbon extraction unit | ||||
| Temperature at the top of the column/. Degree.C | 80 | 85 | 80 | 85 |
| Bottom temperature/°c | 170 | 175 | 170 | 175 |
| pressure/MPa | 0.41 | 0.53 | 0.41 | 0.53 |
| Product distribution/% | ||||
| Cracked gas | 19.13 | 20.56 | 17.56 | 18.36 |
| Benzene | 5.41 | 6.35 | 3.85 | 1.65 |
| Toluene (toluene) | 19.68 | 21.88 | 12.33 | 8.76 |
| Xylene (P) | 28.35 | 31.75 | 18.69 | 14.25 |
| Sum of light aromatic hydrocarbons | 53.44 | 59.98 | 34.87 | 24.66 |
Claims (19)
1. A catalytic conversion process for producing C6 to C8 light aromatic hydrocarbons comprising:
s1, introducing raw oil into a raw material separation unit to obtain a first component rich in polycyclic aromatic hydrocarbon and a second component rich in monocyclic aromatic hydrocarbon;
S2, introducing the first component rich in the polycyclic aromatic hydrocarbon into a hydrotreating unit, carrying out hydrogenation reaction under the action of a hydrogenation catalyst, introducing the obtained hydrogenation component into a catalytic cracking unit, and contacting and reacting with a catalytic cracking catalyst in a catalytic cracking reactor of the catalytic cracking unit;
s3, introducing the second component rich in the monocyclic aromatic hydrocarbon into the catalytic cracking unit, and enabling the second component to contact with a catalytic cracking catalyst in the catalytic cracking reactor and react;
s4, introducing the reaction oil gas generated by the catalytic cracking unit into a product separation unit for separation to respectively obtain cracked gas, light aromatic fraction, heavy aromatic fraction, circulating oil fraction and heavy oil fraction;
s5, introducing the heavy aromatic fraction into the catalytic cracking unit, and enabling the heavy aromatic fraction to contact with a catalytic cracking catalyst in the catalytic cracking reactor and react;
s6, introducing the light aromatic fraction into an aromatic extraction unit for extraction to obtain C6-C8 light aromatic and raffinate oil respectively.
2. The catalytic conversion process of claim 1, wherein the raffinate oil is also introduced to the catalytic cracking unit.
3. The catalytic conversion process according to claim 2, wherein the mixed fraction obtained by mixing the raffinate oil with the heavy aromatic fraction, the second component rich in monocyclic aromatic hydrocarbon and the hydrogenation component are fed at different positions of the catalytic cracking reactor, and the mixed fraction feed inlet, the second component feed inlet rich in monocyclic aromatic hydrocarbon and the hydrogenation component feed inlet are sequentially arranged from bottom to top.
4. A catalytic conversion process according to claim 3, wherein the height of the mixed fraction feed inlet from the bottom of the catalytic cracking reactor is 0 to 1/4, preferably 0 to 1/6 of the total height of the catalytic cracking reactor; the height of the second component feed inlet rich in monocyclic aromatic hydrocarbon from the bottom of the catalytic cracking reactor accounts for 1/4 to 1/3, preferably 1/4 to 2/7 of the total height of the catalytic cracking reactor; the height of the hydrogenation component feed inlet from the bottom of the catalytic cracking reactor is 1/3-2/3, preferably 1/3-1/2 of the total height of the catalytic cracking reactor.
5. The catalytic conversion process of claim 2, wherein the raffinate oil, the heavy aromatic fraction, the mixed fraction of the second component enriched in monocyclic aromatic hydrocarbons, and the hydrogenation component are fed at different locations of the catalytic cracking reactor, in a sequence of a mixed fraction feed inlet and a hydrogenation component feed inlet from bottom to top.
6. The catalytic conversion process according to claim 5, wherein the height of the mixed fraction feed inlet from the bottom of the catalytic cracking reactor is 0 to 1/3, preferably 0 to 1/5, of the total height of the catalytic cracking reactor, and the height of the hydrogenation component feed inlet from the bottom of the catalytic cracking reactor is 1/3 to 2/3, preferably 1/3 to 1/2, of the total height of the catalytic cracking reactor.
7. The catalytic conversion process of any one of claims 1-5, wherein the amount of polycyclic aromatic hydrocarbons in the polycyclic aromatic hydrocarbon rich first component is 70-100 wt%, preferably 80-100 wt%; the amount of monocyclic aromatic hydrocarbon in the second component rich in monocyclic aromatic hydrocarbon is 50 to 100% by weight, preferably 70 to 100% by weight.
8. The catalytic conversion process according to any one of claims 1-5, wherein the feedstock separation unit employs a combination of one or more of distillative separation, adsorptive separation, extractive separation, membrane separation.
9. The catalytic conversion process according to claim 8, wherein the cut point of the first polycyclic aromatic hydrocarbon-rich component and the second monocyclic aromatic hydrocarbon-rich component is 230 to 270 ℃, preferably 240 to 260 ℃, when the feedstock separation unit separates by distillation.
10. The catalytic conversion process according to claim 1, wherein the light aromatic fraction and the heavy aromatic fraction have a cut point of 150-190 ℃, preferably 160-180 ℃; the cutting point of the heavy aromatic fraction and the circulating oil fraction is 200-270 ℃, preferably 230-260 ℃; the cutting point of the cycle oil fraction and the heavy oil fraction is 340 to 370 ℃, preferably 350 to 360 ℃.
11. The catalytic conversion process according to claim 1, wherein the content of C6-C8 aromatics in the light aromatic fraction is not less than 40 wt%, preferably not less than 50 wt%; the content of c9+ aromatic hydrocarbons in the heavy aromatic fraction is not less than 50 wt%, preferably not less than 70 wt%.
12. The catalytic conversion process according to claim 1, wherein the reaction temperature of the hydrotreating unit is 340 to 460 ℃, hydrogen partial pressure is 5 to 15MPa, volume space velocity is 2 to 15h -1 Hydrogen oil volume ratio of 400-1600 Nm 3 /m 3 。
13. The catalytic conversion process according to claim 1, wherein the content of polycyclic aromatic hydrocarbons in the hydrogenation component is not more than 20 wt%, preferably not more than 10 wt%.
14. The catalytic conversion process according to claim 1, wherein the catalytic cracking reactor has a reaction temperature of 520 to 720 ℃, preferably 560 to 640 ℃, a catalyst to oil mass ratio of 1 to 50, preferably 4 to 20, an oil gas residence time of 0.5 to 10s, preferably 0.8 to 6s, and a reaction pressure (gauge pressure) of 0 to 0.2MPa, preferably 0 to 0.15MPa.
15. The catalytic conversion process according to claim 1, wherein the aromatic hydrocarbon extraction unit has a top temperature of 70 to 100 ℃, preferably 80 to 90 ℃, a bottom temperature of 160 to 190 ℃, preferably 170 to 180 ℃, and a pressure (gauge pressure) of 0.25 to 0.6MPa, preferably 0.35 to 0.55MPa.
16. The catalytic conversion process according to claim 1, wherein the extraction solvent used in the aromatic hydrocarbon extraction unit is one or more of sulfolane, N-methylpyrrolidone, dimethyl sulfoxide and formylmorpholine.
17. The catalytic conversion process according to claim 1, wherein the sum of benzene, toluene and xylene content in the C6-C8 light aromatics obtained by the aromatics extraction unit is not less than 95 wt%, preferably not less than 98 wt%.
18. The catalytic conversion process of claim 1, wherein the cycle oil fraction is further introduced into the hydroprocessing unit for hydrogenation; and/or the number of the groups of groups,
and introducing heavy aromatic hydrocarbon fractions generated by other devices into the catalytic cracking reactor for reaction, wherein the other devices comprise one or more of a steam cracking device, a catalytic cracking device, a hydrogenation device, a reforming device and an aromatization device.
19. The catalytic conversion process of claim 1, wherein the feedstock oil is one or more of straight run diesel, catalytically cracked light cycle oil, coker diesel, thermally cracked diesel, aromatizer diesel coal direct liquification diesel, shale oil diesel.
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN103525458A (en) * | 2012-07-06 | 2014-01-22 | 中国石油化工股份有限公司 | Catalytic conversion method |
| CN105085135A (en) * | 2014-05-14 | 2015-11-25 | 中国石油化工股份有限公司 | Method for direct production of benzene and xylene from inferior heavy aromatics |
| CN113462430A (en) * | 2020-03-30 | 2021-10-01 | 中国石油化工股份有限公司 | Method for producing low-carbon olefin and multiple aromatic hydrocarbons from petroleum hydrocarbons |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103525458A (en) * | 2012-07-06 | 2014-01-22 | 中国石油化工股份有限公司 | Catalytic conversion method |
| CN105085135A (en) * | 2014-05-14 | 2015-11-25 | 中国石油化工股份有限公司 | Method for direct production of benzene and xylene from inferior heavy aromatics |
| CN113462430A (en) * | 2020-03-30 | 2021-10-01 | 中国石油化工股份有限公司 | Method for producing low-carbon olefin and multiple aromatic hydrocarbons from petroleum hydrocarbons |
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