CN117004430A - Method and device for producing low-aromatic diesel oil and aromatic hydrocarbon - Google Patents
Method and device for producing low-aromatic diesel oil and aromatic hydrocarbon Download PDFInfo
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- CN117004430A CN117004430A CN202210455650.XA CN202210455650A CN117004430A CN 117004430 A CN117004430 A CN 117004430A CN 202210455650 A CN202210455650 A CN 202210455650A CN 117004430 A CN117004430 A CN 117004430A
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- 150000004945 aromatic hydrocarbons Chemical class 0.000 title claims abstract description 154
- 239000002283 diesel fuel Substances 0.000 title claims abstract description 61
- 238000000034 method Methods 0.000 title claims abstract description 59
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 164
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 78
- 238000000605 extraction Methods 0.000 claims abstract description 67
- 238000011084 recovery Methods 0.000 claims abstract description 61
- 238000005406 washing Methods 0.000 claims abstract description 40
- 238000005194 fractionation Methods 0.000 claims abstract description 22
- 125000003118 aryl group Chemical group 0.000 claims abstract description 16
- 125000005575 polycyclic aromatic hydrocarbon group Chemical group 0.000 claims abstract description 14
- 238000004519 manufacturing process Methods 0.000 claims abstract description 9
- 239000002904 solvent Substances 0.000 claims description 76
- 238000010992 reflux Methods 0.000 claims description 29
- 239000000203 mixture Substances 0.000 claims description 26
- 239000002994 raw material Substances 0.000 claims description 22
- 239000000463 material Substances 0.000 claims description 9
- 238000009835 boiling Methods 0.000 claims description 8
- RGSFGYAAUTVSQA-UHFFFAOYSA-N Cyclopentane Chemical compound C1CCCC1 RGSFGYAAUTVSQA-UHFFFAOYSA-N 0.000 claims description 6
- RTZKZFJDLAIYFH-UHFFFAOYSA-N Diethyl ether Chemical compound CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 claims description 6
- HXJUTPCZVOIRIF-UHFFFAOYSA-N sulfolane Chemical compound O=S1(=O)CCCC1 HXJUTPCZVOIRIF-UHFFFAOYSA-N 0.000 claims description 6
- 238000004064 recycling Methods 0.000 claims description 5
- -1 alkyl sulfolane Chemical compound 0.000 claims description 4
- DMEGYFMYUHOHGS-UHFFFAOYSA-N heptamethylene Natural products C1CCCCCC1 DMEGYFMYUHOHGS-UHFFFAOYSA-N 0.000 claims description 4
- 238000002156 mixing Methods 0.000 claims description 4
- 230000003197 catalytic effect Effects 0.000 claims description 3
- 239000003208 petroleum Substances 0.000 claims description 3
- 238000005201 scrubbing Methods 0.000 claims description 3
- XDTMQSROBMDMFD-UHFFFAOYSA-N Cyclohexane Chemical compound C1CCCCC1 XDTMQSROBMDMFD-UHFFFAOYSA-N 0.000 claims description 2
- 150000002430 hydrocarbons Chemical class 0.000 claims description 2
- 239000003921 oil Substances 0.000 description 79
- 230000000052 comparative effect Effects 0.000 description 18
- 230000000694 effects Effects 0.000 description 10
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 9
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 9
- CMJLMPKFQPJDKP-UHFFFAOYSA-N 3-methylthiolane 1,1-dioxide Chemical group CC1CCS(=O)(=O)C1 CMJLMPKFQPJDKP-UHFFFAOYSA-N 0.000 description 7
- 238000000926 separation method Methods 0.000 description 7
- 238000005265 energy consumption Methods 0.000 description 6
- HYBBIBNJHNGZAN-UHFFFAOYSA-N furfural Chemical group O=CC1=CC=CO1 HYBBIBNJHNGZAN-UHFFFAOYSA-N 0.000 description 6
- 238000010168 coupling process Methods 0.000 description 5
- 239000007789 gas Substances 0.000 description 5
- 238000005984 hydrogenation reaction Methods 0.000 description 5
- 238000001179 sorption measurement Methods 0.000 description 4
- SECXISVLQFMRJM-UHFFFAOYSA-N N-Methylpyrrolidone Chemical compound CN1CCCC1=O SECXISVLQFMRJM-UHFFFAOYSA-N 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 230000005501 phase interface Effects 0.000 description 3
- 238000000746 purification Methods 0.000 description 3
- 238000007670 refining Methods 0.000 description 3
- QPUYECUOLPXSFR-UHFFFAOYSA-N 1-methylnaphthalene Chemical compound C1=CC=C2C(C)=CC=CC2=C1 QPUYECUOLPXSFR-UHFFFAOYSA-N 0.000 description 2
- VZSRBBMJRBPUNF-UHFFFAOYSA-N 2-(2,3-dihydro-1H-inden-2-ylamino)-N-[3-oxo-3-(2,4,6,7-tetrahydrotriazolo[4,5-c]pyridin-5-yl)propyl]pyrimidine-5-carboxamide Chemical compound C1C(CC2=CC=CC=C12)NC1=NC=C(C=N1)C(=O)NCCC(N1CC2=C(CC1)NN=N2)=O VZSRBBMJRBPUNF-UHFFFAOYSA-N 0.000 description 2
- CIWBSHSKHKDKBQ-JLAZNSOCSA-N Ascorbic acid Chemical compound OC[C@H](O)[C@H]1OC(=O)C(O)=C1O CIWBSHSKHKDKBQ-JLAZNSOCSA-N 0.000 description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- IAZDPXIOMUYVGZ-UHFFFAOYSA-N Dimethylsulphoxide Chemical compound CS(C)=O IAZDPXIOMUYVGZ-UHFFFAOYSA-N 0.000 description 2
- LTEQMZWBSYACLV-UHFFFAOYSA-N Hexylbenzene Chemical compound CCCCCCC1=CC=CC=C1 LTEQMZWBSYACLV-UHFFFAOYSA-N 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 2
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical compound CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 description 2
- 239000003463 adsorbent Substances 0.000 description 2
- 230000008878 coupling Effects 0.000 description 2
- 238000005859 coupling reaction Methods 0.000 description 2
- 125000001511 cyclopentyl group Chemical group [H]C1([H])C([H])([H])C([H])([H])C([H])(*)C1([H])[H] 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- LCEDQNDDFOCWGG-UHFFFAOYSA-N morpholine-4-carbaldehyde Chemical compound O=CN1CCOCC1 LCEDQNDDFOCWGG-UHFFFAOYSA-N 0.000 description 2
- 238000000638 solvent extraction Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- 239000008096 xylene Substances 0.000 description 2
- BCNBMSZKALBQEF-UHFFFAOYSA-N 1,3-dimethylpyrrolidin-2-one Chemical compound CC1CCN(C)C1=O BCNBMSZKALBQEF-UHFFFAOYSA-N 0.000 description 1
- WKFQMDFSDQFAIC-UHFFFAOYSA-N 2,4-dimethylthiolane 1,1-dioxide Chemical compound CC1CC(C)S(=O)(=O)C1 WKFQMDFSDQFAIC-UHFFFAOYSA-N 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 1
- 239000005977 Ethylene Substances 0.000 description 1
- AFCARXCZXQIEQB-UHFFFAOYSA-N N-[3-oxo-3-(2,4,6,7-tetrahydrotriazolo[4,5-c]pyridin-5-yl)propyl]-2-[[3-(trifluoromethoxy)phenyl]methylamino]pyrimidine-5-carboxamide Chemical compound O=C(CCNC(=O)C=1C=NC(=NC=1)NCC1=CC(=CC=C1)OC(F)(F)F)N1CC2=C(CC1)NN=N2 AFCARXCZXQIEQB-UHFFFAOYSA-N 0.000 description 1
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 239000000084 colloidal system Substances 0.000 description 1
- 239000002131 composite material Substances 0.000 description 1
- 125000000113 cyclohexyl group Chemical group [H]C1([H])C([H])([H])C([H])([H])C([H])(*)C([H])([H])C1([H])[H] 0.000 description 1
- 230000009849 deactivation Effects 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- KWKXNDCHNDYVRT-UHFFFAOYSA-N dodecylbenzene Chemical compound CCCCCCCCCCCCC1=CC=CC=C1 KWKXNDCHNDYVRT-UHFFFAOYSA-N 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 239000002808 molecular sieve Substances 0.000 description 1
- 125000002950 monocyclic group Chemical group 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 125000001997 phenyl group Chemical group [H]C1=C([H])C([H])=C(*)C([H])=C1[H] 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 1
- 238000004230 steam cracking Methods 0.000 description 1
- 150000003462 sulfoxides Chemical class 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 238000010998 test method Methods 0.000 description 1
- CXWXQJXEFPUFDZ-UHFFFAOYSA-N tetralin Chemical compound C1=CC=C2CCCCC2=C1 CXWXQJXEFPUFDZ-UHFFFAOYSA-N 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
- C10G21/02—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents with two or more solvents, which are introduced or withdrawn separately
- C10G21/04—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents with two or more solvents, which are introduced or withdrawn separately by introducing simultaneously at least two immiscible solvents counter-current to each other
-
- 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
- C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
- C10G21/06—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents characterised by the solvent used
- C10G21/12—Organic compounds only
- C10G21/22—Compounds containing sulfur, selenium, or tellurium
-
- 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
- C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
- C10G21/28—Recovery of used solvent
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
A method and a device for producing low-aromatic diesel oil and aromatic hydrocarbon are characterized in that the production method is carried out in a device comprising an extraction tower (101), a raffinate oil water washing tower (102), a stripping tower (103), an aromatic hydrocarbon recovery tower (104), a water fractionation tower (106) and a stripping agent stripping tower (107). The method couples back extraction and water washing processes, optimizes water circulation, fully utilizes steam stripping energy, and can obtain low aromatic diesel oil with polycyclic aromatic hydrocarbon content not more than 1 mass% and aromatic hydrocarbon product with purity higher than 95 mass% and yield higher than 85 mass%.
Description
Technical Field
The invention relates to a method and a device for producing low-aromatic diesel oil and aromatic hydrocarbon. In particular to a method and a device for producing low-aromatic diesel and aromatic hydrocarbon by separating aromatic hydrocarbon from diesel fraction by using a selective solvent.
Background
In recent years, the market status of diesel oil in China presents a new situation. On one hand, the diesel oil demand is accelerated slowly, the consumption is increased negatively for many times in the past year 2014, and meanwhile, the domestic oil refining scale is continuously expanded, and the phenomenon of excessive diesel oil productivity is increasingly highlighted; on the other hand, the quality standard of the diesel oil for vehicles is continuously improved, and in order to reduce the emission of tail gas pollutants of the diesel engine, the latest national VI diesel oil standard reduces the volume fraction of the polycyclic aromatic hydrocarbon from 11% to 7%. Therefore, reducing the aromatic hydrocarbon content, particularly the polycyclic aromatic hydrocarbon content, in diesel oil and converting the excess diesel oil into chemical raw materials has become an important subject of domestic oil refining process research.
The diesel oil in China mainly comprises three parts of straight-run diesel oil, catalytic diesel oil and coked diesel oil, and the proportion of the diesel oil in a diesel oil tank is 59%, 30% and 11% respectively. The diesel oil from different sources has different compositions, and the aromatic hydrocarbon content of the three diesel oils is about 25%, 70% and 35% respectively. The monocyclic and polycyclic aromatic hydrocarbon not only reduces the cetane number of diesel oil and affects the service performance of the diesel oil, but also can lead to the deactivation of carbon deposition and the loss of components with high cetane number of catalysts used in the subsequent deep processing processes such as refining and reform. Therefore, the aromatic hydrocarbon in the diesel oil is firstly separated by adopting a proper process, so that the quality of the diesel oil can be improved, the obtained low-aromatic diesel oil can be used as an ethylene steam cracking raw material, and aromatic hydrocarbon products separated from the diesel oil can also be used as aromatic hydrocarbon production raw materials to increase the yield of high-added-value chemicals such as ethylene, propylene, benzene, toluene and xylene, thereby providing an economic and feasible method for solving the problem of excessive diesel oil productivity.
At present, the methods for separating aromatic hydrocarbon in diesel mainly comprise a hydrogenation method and a non-hydrogenation method. The conventional diesel hydrogenation process can obviously reduce the aromatic hydrocarbon content, but has the problems of high device investment, severe operating conditions (the temperature is 320-410 ℃, the pressure is 814 MPa), large hydrogen consumption, high loss of non-aromatic hydrocarbon components and the like; the non-hydrogenation method comprises extraction, adsorption and other technical routes.
CN87107146a discloses a method for extracting aromatic hydrocarbon in diesel oil fraction by using double solvents, the boiling range of the diesel oil fraction is 300-530 ℃, the first solvent is selected from furfural, phenol, sulfoxide and dimethyl pyrrolidone, preferably furfural, and the second solvent is light oil, the method can obtain heavy aromatic hydrocarbon with purity higher than 95 mass%, and the extraction rate of aromatic hydrocarbon is 50-95 mass%. The boiling point range of the solvent is far lower than that of the raw material, so that the solvent recovery can be realized by flash evaporation and steam stripping, but the method cannot realize the recovery and utilization of steam stripping, so that a large amount of wastewater containing solvent (furfural) is generated, the energy consumption is high, the solvent loss is serious, and the method is not friendly to the environment.
CN101921624a discloses a method for preparing high-quality diesel oil by an extraction hydrogenation combined process, wherein an extraction solvent is selected from sulfolane, N-methylpyrrolidone and dimethyl sulfoxide, a solvent in raffinate oil is separated by water washing, and separation of the solvent in extract oil and aromatic hydrocarbon is realized by back extraction, water washing and rectification. However, this patent does not disclose a stripping agent and a method for purifying the residual oil water wash and the extracted oil water wash. For diesel fraction aromatic hydrocarbon extraction, the water washing water consumption is obviously higher than that of the gasoline fraction aromatic hydrocarbon (namely benzene, toluene and xylene) extraction process, if the process is not optimally designed, the steam heat is not reasonably utilized, and the energy consumption required for purifying the water can greatly increase the energy consumption of the whole process.
CN105542835a discloses a method for separating polycyclic aromatic hydrocarbon from diesel oil fraction by using simulated moving bed adsorption, the method adopts molecular sieve, oxide or metal modified material as adsorbent, diesel oil fraction firstly removes colloid, sulfur and nitrogen and other impurities by pretreatment adsorbent, then passes through simulated moving bed for adsorption separation, and separated product is rectified to recover desorbent, finally clean diesel oil component and polycyclic aromatic hydrocarbon component are obtained. The content of polycyclic aromatic hydrocarbon in the clean diesel oil component obtained by the method is higher than 1 mass percent, and the aromatic hydrocarbon content of the polycyclic aromatic hydrocarbon component is 83.42-92.18 mass percent. Compared with solvent extraction, the adsorption separation method has high investment cost.
Disclosure of Invention
When low-aromatic diesel oil and aromatic hydrocarbon are produced by separating aromatic hydrocarbon in diesel oil fraction by solvent extraction method, the solvent and the diesel oil fraction are contacted to obtain extract oil containing solvent and aromatic hydrocarbon, the solvent and aromatic hydrocarbon in the extract oil are required to be separated to obtain aromatic hydrocarbon product and recycled solvent which can be recycled, and the lower the aromatic hydrocarbon content in the recycled solvent is, the better. Because of the wide boiling range of the diesel fraction, overlapping the boiling point of aromatic hydrocarbon extraction solvents (e.g., sulfolane, N-formyl morpholine, N-methyl pyrrolidone), the solvent in the extracted oil cannot be separated from the aromatic hydrocarbon by simple rectification. In the prior art, various methods such as water washing, back extraction, steam stripping and the like are adopted to separate the solvent from aromatic hydrocarbon in the extracted oil so as to ensure the purity of the recovered solvent and avoid solvent loss, but the required equipment is large in quantity, the process is complex, and the energy consumption in the water purification process is high.
The inventor finds that the stripping and the water washing process are coupled when the solvent in the extracted oil and the aromatic hydrocarbon are separated, namely the stripping agent and the water are added into the extracted oil at the same time, so that the stripping and the water washing are carried out at the same time, the stripping separation effect can be enhanced, the content of the aromatic hydrocarbon in the obtained recovered solvent is lower than that in the serial process of stripping before water washing, and the separation effect is better.
The inventor also found that by introducing the top water of the aromatic hydrocarbon recovery tower into the raffinate oil water washing tower, the back extraction tower and the water fractionation tower respectively, introducing the steam obtained from the top of the water fractionation tower into the aromatic hydrocarbon recovery tower as stripping gas, so that the solvent recovery and the water purification process are combined, the water circulation can be optimized, the energy of the stripping steam can be fully utilized, and the energy consumption of the whole process can be further reduced.
It is an object of the present invention to provide a process for producing low aromatic diesel and aromatic hydrocarbons. In particular to a method for producing low-aromatic diesel and aromatic hydrocarbon by separating aromatic hydrocarbon from diesel fraction by using a selective solvent. The method couples back extraction and water washing processes, optimizes water circulation, fully utilizes steam stripping energy, and can obtain low aromatic diesel oil with polycyclic aromatic hydrocarbon content not more than 1 mass% and aromatic hydrocarbon product with purity higher than 95 mass% and yield higher than 85 mass%.
The method is characterized by comprising an extraction tower 101, a raffinate oil water scrubber 102, a back extraction tower 103, an aromatic hydrocarbon recovery tower 104, a water fractionating tower 106 and a back extractant fractionating tower 107;
countercurrent contact is carried out between the raw material 1 and the solvent 2 in the extraction tower 101 to obtain an extracted oil 6 and an raffinate oil 3;
introducing the raffinate oil 3 and the raffinate oil 4 into a raffinate oil water scrubber 102 for water scrubbing to obtain low-aromatic diesel oil and scrubbed water 7;
mixing the extracted oil 6 with the washed water 7, introducing the mixture into a stripping tower 103, introducing a stripping agent 9 into the stripping tower 103, introducing water 8 into the stripping tower 103, introducing a material flow obtained from the top of the tower into an aromatic hydrocarbon recovery tower 104 after stripping, and introducing a material flow obtained from the bottom of the tower into a stripping agent stripping tower 107;
aromatic hydrocarbons are obtained at the bottom of the aromatic hydrocarbon recovery tower 104, and a stripping agent 9 and water 13 are obtained at the top of the aromatic hydrocarbon recovery tower;
the stripping agent 19 obtained from the top of the stripping agent stripping tower 107 enters a water fractionating tower 106 from the bottom stream;
all or part of the vapor 14 obtained from the top of the water fractionating tower 106 enters the bottom of the aromatic hydrocarbon recovery tower 104 as stripping gas, and the purified solvent obtained from the bottom of the tower returns to the extraction tower 101 for recycling.
Another object of the present invention is to provide an apparatus for producing low aromatic diesel and aromatic hydrocarbon, which is characterized in that the apparatus comprises an extraction tower 101, a raffinate oil water scrubber 102, a stripping tower 103, an aromatic hydrocarbon recovery tower 104, an aromatic hydrocarbon recovery tower reflux tank 105, a water fractionation tower 106, a stripping agent stripping tower 107, and a stripping agent stripping tower reflux tank 108;
the top of the extraction tower 101 is connected with the raffinate oil washing tower 102 through a pipeline, and the bottom pipeline is connected with the lower part of the stripping tower 103 through a pipeline after being converged with the bottom pipeline of the raffinate oil washing tower 102;
the top of the stripping tower 103 is connected with the aromatic hydrocarbon recovery tower 104 through a pipeline, and the bottom of the stripping tower 103 is connected with the stripping agent stripping tower 107 through a pipeline;
the top of the aromatic hydrocarbon recovery tower 104 is connected with an aromatic hydrocarbon recovery tower reflux tank 105 through a pipeline, the water drum of the aromatic hydrocarbon recovery tower reflux tank 105 is respectively connected with the raffinate oil water scrubber 102, the water fractionation tower 106 and the stripping tower 103 through pipelines, and the bottom pipeline of the aromatic hydrocarbon recovery tower reflux tank 105 is connected with the upper part of the stripping tower 103 through a pipeline after being converged with the bottom pipeline of the stripping agent extraction tower reflux tank 108;
the top of the stripping agent stripping tower 107 is connected with a back-extraction agent stripping tower reflux tank 108 through a pipeline, and the bottom of the stripping agent stripping tower is connected with the water fractionation tower 106 through a pipeline;
the top of the water fractionating tower 106 is connected with the lower part of the aromatic hydrocarbon recovery tower 104 through a pipeline, and the bottom of the water fractionating tower is connected with the upper part of the extraction tower 101 through a pipeline.
The invention provides a method for producing low-aromatic diesel oil and aromatic hydrocarbon, which has the following characteristics:
(1) The purity of the aromatic hydrocarbon product is more than 95 mass percent, and the yield is more than 85 mass percent; the content of polycyclic aromatic hydrocarbon in the low aromatic diesel oil is not more than 1 mass percent.
(2) The optimized back extraction and water purification process is adopted, so that the energy consumption is low, and no wastewater is discharged.
(3) The technological operation condition is mild, no hydrogen consumption is caused, and the investment cost is low.
Drawings
FIG. 1 is a schematic flow chart of a process for separating aromatic hydrocarbons from a diesel fraction according to the present invention.
In fig. 1, extraction column 101, raffinate oil water wash column 102, stripping column 103, aromatic hydrocarbon recovery column 104, aromatic hydrocarbon recovery column reflux drum 105, water fractionation column 106, stripping agent stripping column 107, stripping agent extraction column reflux drum 108, raw material 1, solvent 2, raffinate oil 3, extract oil 6, wash water 7, water 4, 8, 13, 15, stripping agent 9, 19, steam 14, stripping agent and water mixture 16, 18, lines 5, 10, 11, 12, 17, 18, 20.
Detailed Description
The invention provides a method for producing low-aromatic diesel oil and aromatic hydrocarbon, which is characterized in that the production method is carried out in a device comprising an extraction tower 101, a raffinate oil water scrubber 102, a stripping tower 103, an aromatic hydrocarbon recovery tower 104, a water fractionating tower 106 and a stripping agent stripping tower 107;
countercurrent contact is carried out between the raw material 1 and the solvent 2 in the extraction tower 101 to obtain an extracted oil 6 and an raffinate oil 3;
introducing the raffinate oil 3 and the raffinate oil 4 into a raffinate oil water scrubber 102 for water scrubbing to obtain low-aromatic diesel oil and scrubbed water 7;
mixing the extracted oil 6 with the washed water 7, introducing the mixture into a stripping tower 103, introducing a stripping agent 9 into the stripping tower 103, introducing water 8 into the stripping tower 103, introducing a material flow obtained from the top of the tower into an aromatic hydrocarbon recovery tower 104 after stripping, and introducing a material flow obtained from the bottom of the tower into a stripping agent stripping tower 107;
the aromatic hydrocarbon is obtained at the bottom of the aromatic hydrocarbon recovery tower 104, the stripping agent 9 and water 13 are obtained at the top of the tower, the stripping agent 9 is returned to the stripping tower 103 for recycling, the water 13 is divided into three parts, the first part of water 4 is introduced into the upper part of the raffinate oil water scrubber 102, the second part of water 8 is introduced into the upper part of the stripping tower, and the third part of water 15 is introduced into the upper part of the water fractionating tower 106;
the stripping agent 19 obtained from the top of the stripping agent stripping tower 107 enters a water fractionating tower 106 from the bottom stream; the vapor 14 obtained from the top of the water fractionation tower 106 is completely fed into the bottom of the aromatic hydrocarbon recovery tower 104 as stripping gas, or is partially fed into the bottom of the aromatic hydrocarbon recovery tower 104 as stripping gas, and the rest is condensed and fed into one or more of a raffinate oil water scrubber (102), a stripping tower (103) and a water fractionation tower (106); the solvent purified at the bottom of the tower is returned to the extraction tower 101 for recycling.
The stripping agent 9 and the stripping agent 19 can be mixed and then returned to the lower part of the stripping tower.
The extraction tower 101 is used for contacting raw materials with a solvent to perform multistage extraction, so that aromatic hydrocarbon in diesel oil is dissolved in the solvent, raffinate oil is obtained at the top of the tower, and extract oil is obtained at the bottom of the tower. The solvent is selected from sulfolane, alkyl sulfolane and their mixture, alkyl sulfolane is 3-methyl sulfolane, 2, 4-dimethyl sulfolane; the solvent may contain 0.5 to 5.0 mass% of water and 0.01 to 1.0 mass% of hydrocarbon compound. The theoretical plate number of the extraction tower is 8-15, the mass ratio of the solvent to the raw material is 1-5, the tower top pressure is 0.2-0.7 MPa (absolute), the solvent inlet temperature is 60-180 ℃, the preferable 80-160 ℃, the raw material inlet temperature is 20-60 ℃, and the tower bottom temperature is 80-130 ℃.
The raffinate oil water scrubber 102 is used for removing solvent in raffinate oil to obtain low aromatic diesel oil. The theoretical plate number of the raffinate oil water washing tower is 2-10, the tower top pressure is 0.4-0.7 MPa (absolute), the mass ratio of the water washing water to the raffinate oil is 0.05-0.5, preferably 0.1-0.3, and the water washing water inlet temperature is 30-80 ℃.
The stripping tower 103 is used for separating aromatic hydrocarbon and solvent in the extracted oil, the stripping agent is selected from one or more of non-aromatic hydrocarbon, preferably petroleum ether, cyclopentane, cyclohexane, C6 non-aromatic hydrocarbon or mixture of C6 and C7 non-aromatic hydrocarbon with boiling point of 40-150 ℃, the C6 non-aromatic hydrocarbon is from raffinate oil obtained by benzene extraction process, and the mixture of C6 and C7 non-aromatic hydrocarbon is from raffinate oil obtained by benzene and toluene extraction process. The theoretical plate number of the stripping tower is 4-12, the tower top pressure is 0.2-0.8 MPa (absolute), the stripping agent inlet temperature is 30-80 ℃, preferably 35-75 ℃, the water inlet temperature is 30-78 ℃, preferably 35-60 ℃, the tower bottom temperature is 40-80 ℃, preferably 35-60 ℃, the mass ratio of the stripping agent to the extracted oil is 0.05-0.8, preferably 0.1-0.6, and the mass ratio of water to the extracted oil is 0.01-0.2, preferably 0.05-0.15.
The aromatic hydrocarbon product is obtained at the bottom of the aromatic hydrocarbon recovery tower 104, the recyclable stripping agent and water are obtained at the top of the tower, the theoretical plate number is 15-40, the tower top pressure is 0.03-0.2 MPa (absolute), the tower bottom temperature is 120-200 ℃, preferably 130-190 ℃, and the reflux ratio (mass) is 0.2-2.
The purified solvent at the bottom of the water fractionating tower (106) can be recycled, the theoretical plate number is 5-30, the tower top pressure (absolute) is 0.03-0.15 MPa, the tower bottom temperature is 90-200 ℃, and the reflux ratio is 0-1.0.
The stripping agent stripping tower 107 is preferably fed from a first tower plate, the stripping agent is obtained from the tower top and can be recycled, the theoretical plate number is 2-10, and the tower top pressure is 0.1-0.2 MPa (absolute); the temperature of the bottom is 110 to 160 ℃, and the content of residual stripping agent in the bottom stream is 0 to 0.5 mass percent, preferably 0 to 0.1 mass percent.
The boiling range of the raw material is 180-380 ℃, and one or more of straight-run diesel oil, catalytic diesel oil or coked diesel oil is preferable, and the aromatic hydrocarbon content in the raw material is 15-80 mass%.
The polycyclic aromatic hydrocarbon refers to aromatic hydrocarbon containing two or more benzene rings.
The invention relates to a device for producing low-aromatic diesel oil and aromatic hydrocarbon, which is characterized by comprising an extraction tower 101, a raffinate oil water washing tower 102, a back extraction tower 103, an aromatic hydrocarbon recovery tower 104, an aromatic hydrocarbon recovery tower reflux tank 105, a water fractionation tower 106, a back extractant stripping tower 107 and a back extractant stripping tower reflux tank 108;
the top of the extraction tower 101 is connected with the raffinate oil washing tower 102 through a pipeline, and the bottom pipeline is connected with the lower part of the stripping tower 103 through a pipeline after being converged with the bottom pipeline of the raffinate oil washing tower 102;
the top of the stripping tower 103 is connected with the aromatic hydrocarbon recovery tower 104 through a pipeline, and the bottom of the stripping tower 103 is connected with the stripping agent stripping tower 107 through a pipeline;
the top of the aromatic hydrocarbon recovery tower 104 is connected with an aromatic hydrocarbon recovery tower reflux tank 105 through a pipeline, the water drum of the aromatic hydrocarbon recovery tower reflux tank 105 is respectively connected with the raffinate oil water scrubber 102, the water fractionation tower 106 and the stripping tower 103 through pipelines, and the bottom pipeline of the aromatic hydrocarbon recovery tower reflux tank 105 is connected with the upper part of the stripping tower 103 through a pipeline after being converged with the bottom pipeline of the stripping agent extraction tower reflux tank 108;
the top of the stripping agent stripping tower 107 is connected with a back-extraction agent stripping tower reflux tank 108 through a pipeline, and the bottom of the stripping agent stripping tower is connected with the water fractionation tower 106 through a pipeline;
the top of the water fractionating tower 106 is connected with the lower part of the aromatic hydrocarbon recovery tower 104 through a pipeline, and the bottom of the water fractionating tower is connected with the upper part of the extraction tower 101 through a pipeline.
The invention is further described below with reference to the drawings.
In FIG. 1, a raw material 1 enters the lower part of an extraction tower 101, a solvent 2 enters the upper part of the tower 101, the solvent 2 and the lower part are in countercurrent contact, extraction oil 6 is obtained at the bottom of the tower, raffinate oil 3 obtained at the top of the tower is introduced into the lower part of a raffinate oil water washing tower 102, water 4 is introduced into the upper part of the water washing tower 102, low-aromatic diesel oil is obtained at the top of the water washing tower 102 through water washing, the low-aromatic diesel oil is discharged through a pipeline 5, washed water 7 obtained at the bottom of the tower is mixed with extraction oil 6 discharged from the bottom of the extraction tower 101 and then introduced into the middle lower part of a stripping tower 103, water 8 is introduced into the upper part of the stripping tower 103, a stripping agent is introduced into the lower part of the stripping tower 103, a stream obtained at the bottom of the stripping tower 103 is introduced into the upper part of a stripping agent stripping tower 107 through a pipeline 12, a stream obtained at the top of the stripping tower 103 is introduced into the middle part of an aromatic hydrocarbon recovery tower 104 through a pipeline 10, the water vapor 14 is introduced into the lower part of an aromatic hydrocarbon recovery tower 104, the aromatic hydrocarbon obtained from the bottom of the aromatic hydrocarbon recovery tower 104 is discharged out of the device through a pipeline 17, a mixture 16 of a stripping agent and water obtained from the top of the aromatic hydrocarbon recovery tower 104 is condensed and enters an aromatic hydrocarbon recovery tower reflux tank 105 to separate oil phase and water, a part of the oil phase is returned to the upper part of the aromatic hydrocarbon recovery tower 104 through a pipeline 11, the rest of the oil phase is the stripping agent 9 and is introduced into the lower part of a stripping tower 103, water 13 separated from a water packet of the aromatic hydrocarbon recovery tower reflux tank 105 is divided into three parts, the first part of water 4 is introduced into the upper part of a raffinate oil water washing tower 102, the second part of water 8 is introduced into the upper part of the stripping tower 103, and the third part of water 15 is introduced into the upper part of a water fractionation tower 106. Condensing a mixture 18 of a stripping agent and water obtained from the top of a stripping agent stripping tower 107, then introducing the mixture into a stripping agent extraction reflux tank 108, discharging the stripping agent 19, mixing the mixture with the stripping agent 9, delivering the mixture to the lower part of a stripping tower 103, introducing a material flow discharged from the bottom of the stripping agent stripping tower 107 into a water fractionating tower 106 through a pipeline 20, rectifying, introducing water vapor 14 obtained from the top of the tower into the lower part of a tower 104, and introducing a solvent 2 discharged from the bottom of the tower into the upper part of a tower 101 for recycling. The invention is further illustrated by the following examples, but is not limited thereto.
Comparative example 1 and example 1 examined the effect of different stripping processes on the results of separating solvent and aromatic hydrocarbons in the extracted oil.
Comparative example 1
Comparative example 1-1 strip
The 3-methyl sulfolane is taken as a solvent to simulate the extracted oil to be reextracted, the composition is shown in table 1, the reextractor is cyclopentane, the reextractor and the extracted oil are fully mixed at 40 ℃, wherein the mass ratio of the reextractor to the extracted oil is 0.5, the reextractor and the extracted oil are placed in a constant temperature oven at 40 ℃ for standing for 2 hours, liquid-liquid two phases with clear phase interfaces are formed, the upper layer is the reextractor and aromatic hydrocarbon, the lower layer is the recovered solvent, and the aromatic hydrocarbon content in the recovered solvent is analyzed, and the result is shown in table 2.
Comparative examples 1-2 Water washing
3-methyl sulfolane is taken as a solvent to simulate the extracted oil to be back extracted, the composition is shown in table 1, water and the extracted oil are fully mixed at 40 ℃, the mass ratio of the water to the extracted oil is 0.1, then the mixture is placed in a constant temperature oven at 40 ℃ for standing for 2 hours to form liquid-liquid two phases with clear phase interfaces, the upper layer is aromatic hydrocarbon, the lower layer is a water-containing recovered solvent, and the content of aromatic hydrocarbon in the recovered solvent is analyzed, so that the results are shown in table 2.
Comparative examples 1 to 3 were back-extracted and then water-washed
The recovered solvent obtained in comparative example 1-1 was washed with water by the method described in comparative example 1-2 to obtain a recovered solvent after back extraction and then washing with water, and the aromatic hydrocarbon content was analyzed, and the results are shown in Table 2.
Example 1
Example 1 stripping-Water washing coupling
3-methyl sulfolane is taken as a solvent to simulate the extracted oil to be stripped, the composition of the extracted oil is shown in table 1, the stripping agent is cyclopentane, and the stripping agent, water and the extracted oil are fully mixed at 40 ℃, wherein the mass ratio of the stripping agent to the water to the extracted oil is 0.5:0.1:1, then placing the mixture in a constant temperature oven at 40 ℃ for standing for 2 hours to form a liquid-liquid two-phase with a clear phase interface, wherein the upper layer is a stripping agent and aromatic hydrocarbon, the lower layer is a water-containing recovery solvent, and the content of aromatic hydrocarbon in the recovery solvent is analyzed, and the result is shown in Table 2.
TABLE 1
| Extracting oil component | Mass fraction% |
| Aromatic hydrocarbons | |
| N-hexylbenzene | 1.05 |
| Tetrahydronaphthalene | 0.89 |
| 1-methylnaphthalene | 1.06 |
| Dodecylbenzene | 1.41 |
| Solvent(s) | |
| 3-methyl sulfolane | 95.59 |
| Totalizing | 100 |
TABLE 2
| Numbering device | Treatment process | Recovering aromatic hydrocarbon content in solvent, mass% |
| Comparative examples 1 to 1 | Back extraction | 1.51 |
| Comparative examples 1 to 2 | Washing with water | 0.92 |
| Comparative examples 1 to 3 | Back extraction and then water washing | 0.54 |
| Example 1 | Back extraction-water washing coupling | 0.38 |
As can be seen from Table 2, the recovered solvent obtained by the water washing-stripping coupling process has the lowest aromatic hydrocarbon content, which indicates that the water washing-stripping coupling process is adopted to separate the solvent from aromatic hydrocarbon in the extracted oil, and the separation effect is optimal.
Example 2 the effect of temperature on the results of stripping-water wash coupling process on solvent and aromatics in separated oil.
Example 2
The stripping agent is cyclohexane, and the simulated extraction oil and the test procedure are the same as in example 1. The temperature of the oven was changed, and the composition was analyzed by taking the lower solvent phase, and the aromatic hydrocarbon content in the recovered solvent after back extraction was obtained as shown in table 5.
TABLE 3 Table 3
As can be seen from table 3, the stripping-washing coupled process at a lower temperature has the lowest aromatic hydrocarbon content in the recovered solvent, the best effect, and the separation effect is poor as the aromatic hydrocarbon content in the recovered solvent increases significantly with increasing temperature.
Examples 3-5 and comparative examples 2-3 examined the effect of different stripping agents and stripping processes on low aromatic diesel and aromatic products.
Example 3
The low aromatic diesel and aromatic hydrocarbon were produced according to the scheme shown in fig. 1, and the raw material properties are shown in table 4. The solvent is 3-methyl sulfolane, the stripping agent is C6 non-aromatic hydrocarbon, the main operation conditions of each tower are shown in Table 5, and the compositions and yields of the low-aromatic diesel and aromatic hydrocarbon products are shown in Table 6.
TABLE 4 Table 4
Example 4
The low-aromatic diesel oil and aromatic hydrocarbon are produced according to the flow shown in fig. 1, the raw material properties are shown in table 4, the solvent is sulfolane and 3-methyl sulfolane composite solvent with the mass ratio of 1:1, the stripping agent is C6-C7 fraction aromatic hydrocarbon extraction raffinate oil, the main operation conditions of each tower are shown in table 5, and the compositions and the yields of the low-aromatic diesel oil and aromatic hydrocarbon products are shown in table 6.
Example 5
The low aromatic diesel and aromatic hydrocarbon were produced according to the procedure shown in fig. 1, the raw material properties are shown in table 4, the solvent is sulfolane, the stripping agent is petroleum ether, the main operating conditions of each column are shown in table 5, and the compositions and yields of the low aromatic diesel and aromatic hydrocarbon products are shown in table 6.
Comparative example 2
The low aromatic diesel and aromatic hydrocarbon were produced according to the scheme shown in fig. 1, and the raw materials were the same as in example 3. The solvent is N-methyl pyrrolidone, the stripping agent is C6 fraction aromatic hydrocarbon extraction raffinate oil, the main operating conditions of each tower are shown in Table 5, and the compositions and yields of the obtained low-aromatic diesel oil and aromatic hydrocarbon products are shown in Table 6.
As can be seen from Table 6, the same raw materials are treated in example 3 and comparative example 2, and the aromatic hydrocarbon product yield and the total aromatic hydrocarbon content are higher in example 3 compared with comparative example 2; the low aromatic diesel oil yield is higher, and the total aromatic hydrocarbon content and the polycyclic aromatic hydrocarbon content in the low aromatic diesel oil are lower, which indicates that the invention obtains better effect.
Comparative example 3
The comparative example adopts a process of back extraction and then water washing to separate aromatic hydrocarbon in diesel oil fraction, and the raw materials, solvent and back extractant are the same as those in example 3. The main operating conditions of each tower are shown in Table 7, and the compositions and yields of the obtained low-aromatic diesel and aromatic hydrocarbon products are shown in Table 6.
As can be seen from table 6, the same raw materials are treated by different processes, the same solvent and the stripping agent in example 3 and comparative example 3, and the aromatic hydrocarbon product yield and the total aromatic hydrocarbon content are higher in example 3 compared with comparative example 3; the low aromatic diesel oil has lower total aromatic hydrocarbon content and polycyclic aromatic hydrocarbon content, which shows that the invention has better effect.
TABLE 5
TABLE 6
TABLE 7
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Claims (16)
1. A method and a device for producing low-aromatic diesel oil and aromatic hydrocarbon are characterized in that the production method is carried out in a device comprising an extraction tower (101), a raffinate oil water washing tower (102), a stripping tower (103), an aromatic hydrocarbon recovery tower (104), a water fractionation tower (106) and a stripping agent stripping tower (107). The method couples back extraction and water washing processes, optimizes water circulation, fully utilizes steam stripping energy, and can obtain low aromatic diesel oil with polycyclic aromatic hydrocarbon content not more than 1 mass% and aromatic hydrocarbon product with purity higher than 95 mass% and yield higher than 85 mass%.
The method for producing the low-aromatic diesel and the aromatic hydrocarbon is characterized in that the production method is carried out in a device comprising an extraction tower (101), a raffinate oil water washing tower (102), a back extraction tower (103), an aromatic hydrocarbon recovery tower (104), a water fractionation tower (106) and a back extraction agent stripping tower (107);
the raw material (1) and the solvent (2) are in countercurrent contact in the extraction tower (101) to obtain extracted oil (6) and raffinate oil (3);
introducing the raffinate oil (3) and the water (4) into a raffinate oil water scrubber (102) for water scrubbing to obtain low-aromatic diesel oil and scrubbed water (7);
mixing the extracted oil (6) with the washed water (7), introducing the mixture into a stripping tower (103), introducing a stripping agent (9) into the stripping tower (103), introducing water (8) into the stripping tower (103), carrying out stripping, introducing a material flow obtained from the top of the tower into an aromatic hydrocarbon recovery tower (104), and introducing a material flow obtained from the bottom of the tower into a stripping agent stripping tower (107);
aromatic hydrocarbons are obtained at the bottom of the aromatic hydrocarbon recovery tower (104), and a stripping agent (9) and water (13) are obtained at the top of the aromatic hydrocarbon recovery tower;
the stripping agent (19) is obtained from the top of the stripping agent stripping tower (107), and the bottom material flow enters a water fractionating tower (106);
all or part of vapor (14) obtained from the top of the water fractionating tower (106) enters the bottom of the aromatic hydrocarbon recovery tower (104) as stripping gas, and the purified solvent obtained from the bottom of the tower returns to the extraction tower (101) for recycling.
2. The method according to claim 1, wherein the water (13) obtained from the top of the aromatic hydrocarbon recovery tower (104) is divided into three parts, wherein the first part of water (4) is introduced into the upper part of the raffinate oil water scrubber (102), the second part of water (8) is introduced into the upper part of the stripping tower, and the third part of water (15) is introduced into the upper part of the water fractionation tower (106).
3. The method according to claim 1, wherein part of the water vapor (14) obtained from the top of the water fractionation column (106) enters the bottom of the aromatic hydrocarbon recovery column (104) as stripping gas, and the rest is condensed and enters one or more of the raffinate oil water scrubber (102), the stripping column (103) and the water fractionation column (106).
4. A process according to claim 1, characterized in that the solvent in the extraction column (101) is selected from sulfolane, alkyl sulfolane and mixtures thereof.
5. The method according to claim 1 or 4, wherein the solvent contains 0.5 to 5.0% by mass of water and 0.01 to 1.0% by mass of a hydrocarbon compound.
6. The process according to claim 1, wherein the stripping agent is a non-aromatic hydrocarbon having a boiling point of 40 to 150 ℃.
7. The process according to claim 1 or 6, wherein the stripping agent is selected from one or more of petroleum ether, cyclopentane, cyclohexane, C6 non-aromatic hydrocarbons or mixtures of C6 and C7 non-aromatic hydrocarbons.
8. The process according to claim 1, wherein in the extraction column (101), the mass ratio of the solvent to the raw material is 1 to 5, the solvent feeding temperature is 60 to 180 ℃, and the column top pressure is 0.2 to 0.7MPa.
9. The process according to claim 1, wherein in the raffinate oil water scrubber (102), the mass ratio of water washing water to raffinate oil is 0.05 to 0.5, the overhead pressure is 0.4 to 0.7MPa, and the water washing water inlet temperature is 30 to 80 ℃.
10. The process according to claim 1, wherein in the stripping column (103), the column top pressure is 0.2-0.8 MPa, the stripping agent inlet temperature is 30-80 ℃, the mass ratio of the stripping agent to the extracted oil is 0.05-0.8, the water (8) inlet temperature is 30-78 ℃, and the mass ratio of the water to the extracted oil is 0.01-0.2.
11. The process according to claim 1, wherein in the aromatic hydrocarbon recovery column (104), the reflux ratio is 0.2 to 2, the column top pressure is 0.03 to 0.2MPa, and the column bottom temperature is 120 to 200 ℃.
12. The process according to claim 1, wherein in the water fractionation column (106), the reflux ratio is 0 to 1.0, the column top pressure is 0.03 to 0.15MPa, and the column bottom temperature is 90 to 200 ℃.
13. The process according to claim 1, wherein in the stripping agent stripping column (107), the column top pressure is 0.1-0.2 MPa and the column bottom temperature is 110-160 ℃.
14. The process of claim 1 wherein said feed boiling range is 180 to 380 ℃.
15. The method according to claim 1 or 14, wherein the feedstock is selected from one or more of straight run diesel, catalytic diesel or coker diesel.
16. The device for producing the low-aromatic diesel oil and the aromatic hydrocarbon is characterized by comprising an extraction tower (101), a raffinate oil washing tower (102), a back extraction tower (103), an aromatic hydrocarbon recovery tower (104), an aromatic hydrocarbon recovery tower reflux tank (105), a water fractionation tower (106), a back extractant stripping tower (107) and a back extractant extraction tower reflux tank (108);
the top of the extraction tower (101) is connected with the raffinate oil washing tower (102) through a pipeline, and the bottom pipeline is connected with the lower part of the stripping tower (103) through a pipeline after being converged with the bottom pipeline of the raffinate oil washing tower (102);
the top of the stripping tower (103) is connected with the aromatic hydrocarbon recovery tower (104) through a pipeline, and the bottom of the stripping tower is connected with the stripping agent stripping tower (107) through a pipeline;
the top of the aromatic hydrocarbon recovery tower (104) is connected with an aromatic hydrocarbon recovery tower reflux tank (105) through a pipeline, a water drum of the aromatic hydrocarbon recovery tower reflux tank (105) is respectively connected with a raffinate oil water scrubber (102), a water fractionation tower (106) and a stripping tower (103) through pipelines, and the bottom pipeline of the aromatic hydrocarbon recovery tower reflux tank (105) is connected with the upper part of the stripping tower (103) through a pipeline after being converged with the bottom pipeline of a stripping agent extraction tower reflux tank (108);
the top of the stripping agent stripping tower (107) is connected with a back flow tank (108) of the stripping agent stripping tower through a pipeline, and the bottom of the stripping agent stripping tower is connected with the water fractionation tower (106) through a pipeline;
the top of the water fractionating tower (106) is connected with the lower part of the aromatic hydrocarbon recovery tower (104) through a pipeline, and the bottom of the water fractionating tower is connected with the upper part of the extraction tower (101) through a pipeline.
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