CN1227330C - Process for removing sulfur and arene from solvent oil - Google Patents
Process for removing sulfur and arene from solvent oil Download PDFInfo
- Publication number
- CN1227330C CN1227330C CN 01108455 CN01108455A CN1227330C CN 1227330 C CN1227330 C CN 1227330C CN 01108455 CN01108455 CN 01108455 CN 01108455 A CN01108455 A CN 01108455A CN 1227330 C CN1227330 C CN 1227330C
- Authority
- CN
- China
- Prior art keywords
- oil
- extraction
- stock oil
- solvent
- sorbent material
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Fats And Perfumes (AREA)
Abstract
The present invention relates to a method for producing solvent oil by nitration-extraction-adsorption desulfurization and dearomatization. Firstly, aromatic hydrocarbon in raw oil is converted into nitration objects by nitric acid and sulphuric acid, and neutral sulfide is oxidized into polar sulfide; secondly, nitration products are extracted by the mixed liquor of organic alkali and low molecule alcohol; finally, residual aromatic hydrocarbon, nitration objects and organic sulfur in oil are eliminated by adsorbent, and the solvent oil products are obtained. The method provided by the present invention is suitable for the desulphurization and dearomatization of the solvent oil with various trademarks, has the advantages of simple equipment, short technological process, easy operation, low operating cost and high economic benefit. The method not only obtains eligible solvent oil, but also obtains diesel oil hexadecane value improvers, hydrochloric acid and side products of polymerizing aluminium sulfate.
Description
Technical field
The present invention relates to a kind of novel method of removing sulfur and arene from solvent oil, belong to the oil purification method.
Background technology
In Chemical Manufacture, solvent oil is the oils that some material is played dissolving, dilution, washing and extraction.It is to be formed by the straight run oil of oil, platformate raffinate or other working method gained distillate treating.The production of solvent oil is distilled cutting to the suitable raw material of selecting, and the crucial controlling index of quality product is aromatic hydrocarbon and total sulfur content.China's solvent oil grade mainly contains soybean extracting solvent no.6, aero-washing gasoline, perfume extraction solvent, sherwood oil, rubber solvent naphtha, detergent solvent naphtha, varnish makers' and painters' naphtha and aluminum foil rolling wet goods.Wherein soybean extracting solvent no.6 is as the edible vegetable oil and fat extraction agent; Perfume extraction solvent is as the special-purpose extraction agent of essence, food flavour and medicine; Aluminum foil rolling oil is processed with aluminium-foil containers as food, beverage, and they are strict to aromatic hydrocarbon and total sulfur content, require aromatic hydrocarbon＜0.1～0.5%, total sulfur＜2ppm with aluminum foil rolling oil especially, and is the harshest.Therefore, the key of solvent oil production is desulfurizing and dearomatizing (longevity Deqing " accumulating oil plant ", press of University of Petroleum, 1998).At present, the technology that is used for removing sulfur and arene from solvent oil both at home and abroad mainly contain following several [Li Fengrong etc. remove the research of aromatic hydrocarbons in the soybean extracting solvent no.6. oilfield surface engineering .12 (5), 1993; Ke Ming etc., the non-hydrogenating desulfurization progress of light-end products. oil and gas chemical industry .26 (2), 1997]:
(1) hydrogenating desulfurization technology: the industrialization already of fraction oil hydrodesulfurizing technology, the subject matter of existence are that industrial scale is big, and investment is high, and hydrogen source must be arranged, and the product sulphur content is still up to tens～hundreds of ppm.Obviously, hydrogenating desulfurization technology can not satisfy the requirement of aluminum foil rolling wet goods special solvent oil to meticulous desulfurization.
(2) catalyzed oxidation technology: with the Merox technology is representative.But this method mainly is that mercaptan sulfur is oxidized to disulphide, and the latter still is present in the oil product, and real is deodorization.The catalyzed oxidation technology can not be used for sulphur content is required the production of harsh solvent oil.
(3) acid-alkali refining: acid-alkali refining is a traditional method.Acid treating is mainly used in desulfurization ether, and soda finishing then is used to take off inorganic sulfur and mercaptan and oxygen acid.Acid-alkali refining exists the soda acid slag difficult, and the oil product loss is big, can not satisfy the requirement of the meticulous desulfurizing and dearomatizing of solvent oil.
(4) solvent extraction: solvent extraction is indoor and the important method of industrial desulfurization.The solvent great majority that use are polar solvent, and as phenol, nitre benzene, nitrophenol, aniline, furfural etc., general desulfurization degree can reach 40～70%.
(5) sulfonation method: sulfonation method is used for solvent oil and takes off aromatic hydrocarbons industrialization already.Existing problems are to use 98% sulfuric acid, oleum or sulphur trioxide, and equipment corrosion is serious, and it is difficult to produce a large amount of acid sludges, kerosene loss amount height.
(6) hydrogenation aromatics-removing: hydrogenation aromatics-removing generally adopts metal catalysts such as Ni, Pd, Mo, and under 400～500 ℃, it is saturated that benzene and homologue thereof are depressed hydrogenation at certain hydrogen branch.But only be only completely, otherwise senior arene compound hydrogenation only trends towards changing into benzene and lower homologue thereof at quite high hydrogen dividing potential drop such as 200atm and above hydrogenation thereof.Moreover the hydrofining industrial scale is big, and investment is high, and hydrogen source must be arranged, and is not suitable for small-scale production.
(7) absorption method: absorption method is industrialization.Generally be with arenes selectivity be adsorbed on the solid adsorbent, to realize separating of aromatic hydrocarbons and non-aromatics.The sorbent material that adopts has silica gel, activated alumina, gac, molecular sieve etc., and wherein molecular sieve is most widely used, especially 13X, 10X type molecular sieve.But the absorption method solvent oil takes off aromatic hydrocarbons and exists industrial scale big, the higher problems such as (reaching as high as 2～3%) of aromaticity content in investment height and the product.
(8) solvent extration: this method industrialization already.The industrialized aromatic hydrocarbons extraction separation method in countries in the world mainly contains Udex method, sulfolane process, N methylpyrrolidone process, dimethyl sulfoxide method and morpholine method.But solvent extration investment and process cost height, complicated operation.The more serious problem that exists is to take off more height of fragrant rate, and the kerosene loss is bigger.
Obviously, existing removing sulfur and arene from solvent oil technology is little for industrial scale, aromatic hydrocarbon and total sulfur content require the production of harsh high-grade solvent oil to have a series of techno-economic question, must seek new removing sulfur and arene from solvent oil technology.
Summary of the invention
The method that the purpose of this invention is to provide a kind of removing sulfur and arene from solvent oil, it is applicable to the removing sulfur and arene from solvent oil of the various trades mark, is method preferably to the strict high-grade solvent oil of aromatic hydrocarbon and total sulfur content such as aluminum foil rolling oil, soybean extracting solvent no.6 and perfume extraction solvent etc. especially.This method not only can obtain up-to-standard solvent oil product, and can obtain products such as by-product diesel cetane-number improver, technical hydrochloric acid and polyaluminium sulfate water conditioner.
The method of a kind of removing sulfur and arene from solvent oil provided by the invention, be to adopt nitrated-extraction-absorption method to produce solvent oil, at first be use by nitric acid and sulfuric acid form take off fragrant agent TJ-1 with the aromatic hydrocarbons in the stock oil be converted into itrated compound (a kind of diesel oil octane promoter), the mitigation of neutral sulfide is oxidized to polarity sulfide; With a kind of extraction agent TJ-2 that forms by organic bases and low mass molecule alcohol mixture, aromatic hydrocarbon itrated compound and polarity sulfide are extracted from stock oil then; Use residual aromatics and itrated compound and whole organosulfur in the sorbent material aluminum trichloride (anhydrous) adsorbing and removing stock oil at last, promptly obtain the solvent oil product.The TJ-2 that will contain the aromatic hydrocarbon itrated compound mixes with a certain amount of kerosene, and heating steams TJ-2 and gets final product, and the aromatic hydrocarbon itrated compound then is dissolved in kerosene and promptly obtains diesel oil octane promoter (cetane number improver) product.With adsorptive hydrolysis, the neutralization of sorbent material aluminum trichloride (anhydrous), the hydrogen chloride gas water of generation absorbs, and promptly obtains technical hydrochloric acid (30%).After wherein nitric acid is reclaimed in TJ-1 resistates distillation, obtain alum liquor with the hydrolyzate neutralization of sorbent material aluminum chloride adsorptive, the latter can further remove synthesized polymer Tai-Ace S 150, a kind of water conditioner product.
Obviously, a kind of removing sulfur and arene from solvent oil technology provided by the invention is made up of the operation stepss such as chemical conversion, extraction, absorption and remaining additive aftertreatment of aromatic hydrocarbon and sulfide, and concrete implementation method is as follows:
(1) chemical conversion of aromatic hydrocarbon and sulfide: get a certain amount of 68% nitric acid and 98% sulfuric acid, press nitric acid and at room temperature mix, promptly obtain taking off fragrant agent TJ-1 with vitriolic mass ratio 1.2～1.7: 1; TJ-1 and stock oil are added constant temperature in 50-60 ℃ stock oil, stirring reaction 25～35min gradually in the ratio of mass ratio 0.10～0.12; With reaction mixture sat 3～8min, nitrated stock oil and remaining TJ-1 promptly are separated, and nitrated stock oil goes extraction test, and remaining TJ-1 then removes to reclaim nitric acid and preparation polyaluminium sulfate.
(2) extraction: with three kinds of C
1-C
3The arbitrary proportion mixture of low mass molecule alcohol and the arbitrary proportion mixture of organic bases more than at least 3 kinds by volume 30～20: 70～80 mix, wherein said organic bases is selected from quadrol, diethylamine, propylene diamine, triethylamine, dipropyl amine or Diisopropylamine, promptly obtains extraction agent TJ-2; Nitrated stock oil and extraction agent TJ-2 are 1～1/2 by volume, mix extraction 3～5min under normal pressure, room temperature～50 ℃; To extract mixture and leave standstill 5～10min, the stock oil of extraction and remaining TJ-2 promptly are separated, and reclaim remaining TJ-2, get fresh TJ-2 again the stock oil that extracts is extracted next time, and extraction times is 3～5 times.
(3) absorption: with the stock oil mass ratio of sorbent material aluminum trichloride (anhydrous) and extraction is that 0.0267 ratio takes by weighing the sorbent material aluminum trichloride (anhydrous), and the back of milling adds rapidly in the stock oil of extraction, airtight, 90 ℃ of constant temperature, settlement separate 20min behind the stirring 30min.The Filtration Adsorption mixture promptly obtains the solvent oil product; Sorbent material resistates (adsorptive) is used to reclaim cetane number improver.
(4) TJ-2 regeneration: remaining TJ-2 was mixed with kerosene in 1: 1 by volume, slowly be heated to 110～120 ℃, constant temperature 2 hours steams extraction agent TJ-2, continues to be warmed up to 190～200 ℃, during constant temperature 30min, stops distillation; Overhead product obtains regeneration TJ-2 through condensation recovery, settlement separate, and distillation residue are the diesel cetane-number improver product that is dissolved in kerosene or diesel oil solvent.
(5) processing of remaining TJ-1 and remaining sorbent material: the water that slowly adds 5 times of quality in the sorbent material resistates is hydrolyzed.The hydrogen chloride gas that hydrolysis produces, water absorbs, and promptly obtains technical hydrochloric acid; Remaining TJ-1 is heated to 90～120 ℃, and distillation recovery nitric acid is used for preparation and takes off fragrant agent TJ-1, and the residuum after the distillation adds the hydrolyzed solution neutralization of sorbent material resistates gradually, obtains the oil-aqueous solution suspension of sulfur acid aluminium salt; Leave standstill the suspension phase-splitting, on be the residual raw materials oil of recovery mutually, can be used as the cetane number improver solvent, filter phase down, filter residue and filtrate, filter residue is the cetane number improver of recovery, filtrate is then removed synthesized polymer Tai-Ace S 150.
Adopt nitrated-extraction-absorption method to produce the cetane number improver of solvent oil process by-product, belong to nitrated oils cetane number improver, domesticly it is in harmonious proportion performance and has carried out a large amount of research.The base oil that adopts has factory of shanghai refinery catalytic cracking diesel oil, Kelamayi refinery catalytic cracking diesel oil and the three-way straight-run diesel oil of normal pressure, Wuhan refinery residual oil catalytic cracking diesel oil, is in harmonious proportion nitrated oils cetane number improver.Result of study shows, in catalytic cracking diesel oil, add the nitrated oils improving agent of 0.1～0.5m%, cetane value can improve 3～7 units, and in containing 10% straight-run diesel oil, interpolation 0.5% can reach the cetane value level of the blended diesel of 60% straight-run diesel oil.[referring to Li Jun etc., the interpolation performance and the mechanism of action of NT-11 diesel cetane-number improver. petroleum journal (refining of petroleum) .9 (2), 1993].
Polyaluminium sulfate is as water conditioner, and its production, use are that a kind of very sophisticated industrial technology is [referring to volumes " inorganic chemicals industry handbook (volume two), Chemical Industry Press, 1996] such as Tianjin chemical research institutes.Polyaluminium sulfate main is used for water, process water, plant drainage processing etc. as water purification agent industrial, is used for makeup, water-resisting agent in addition, adds material, medicine, adds sulphur promotor etc.Quote water, process water and flocculant for treating waste water.Industrial process has aluminium hydroxide method, Tai-Ace S 150 method, ion exchange method, alkaline process, sodium aluminate method etc., and the present invention selects for use the Tai-Ace S 150 legal system to be equipped with polyaluminium sulfate.
The method of a kind of removing sulfur and arene from solvent oil provided by the invention has following advantage: it is applicable to the removing sulfur and arene from solvent oil of the various trades mark (1), especially to aromatic hydrocarbon and the strict high-grade solvent oil of total sulfur content.Do not have the stock oil loss when (2) the present invention has industrial production, stock oil is converted into three portioned products: solvent oil, (aromatic hydrocarbons is converted into) diesel oil octane promoter, octane promoter solvent, and organosulfur all enters octane promoter; (3) the formant operating equipment is simple, and industrial flow is short, characteristics such as easy to operate and investment, process cost are low, economic benefit height.(4) this method not only can obtain up-to-standard solvent oil product, and can access byproducts such as diesel cetane-number improver, technical hydrochloric acid and polyaluminium sulfate water conditioner.
Specific implementation method
The present invention is further illustrated below by several embodiment.
Embodiment 1: get 68% nitric acid 9g, 98% sulfuric acid 6g, at room temperature slowly mix, promptly obtain 15g and take off fragrant agent TJ-1; Get low mass molecule alcohol l00ml (wherein methyl alcohol 20ml, ethanol 50ml and Virahol 30ml), organic bases 300ml (wherein quadrol 20ml, diethylamine 45ml, propylene diamine 45ml, triethylamine 80ml, dipropyl amine 30ml, Diisopropylamine 80ml), by pure: alkali (volume ratio)=mix at 25: 75 promptly gets 400ml extraction TJ-2.Ratio in TJ-1/ stock oil (mass ratio)=0.11, get and take off fragrant agent 11g and add among 170～260 ℃ of straight run kerosene 100g (constant temperature is 50～60 ℃) that contain aromatic hydrocarbons 5.58%, total sulfur 765ppm by Nanchong oil-refining chemical head factory production stirring reaction 30min gradually; With reaction mixture sat 5min, nitrated stock oil and remaining TJ-1 promptly are separated; With TJ-2 and nitrated stock oil is 2/3 by volume, gets extraction agent 80ml at normal pressure, room temperature～50 ℃ down and nitrated stock oil hybrid extraction 5min, leaves standstill phase-splitting 10min, and the stock oil of extraction and remaining TJ-2 promptly are separated, and extract 4 times repeatedly to get final product; In the stock oil mass ratio of sorbent material aluminum trichloride (anhydrous) and extraction is that 0.0267 ratio takes by weighing sorbent material 2.53g, and the back of milling adds rapidly in the stock oil of extraction, airtight, 90 ℃ of constant temperature, and sedimentation 20min separates behind the vigorous stirring 30min.The Filtration Adsorption mixture promptly obtains high-grade solvent oil-aluminum foil rolling oil production 92.8g, through complete aromatic free of mass spectroscopy product and organosulfur compound, reaches solvent oil product quality indicator (aromatic hydrocarbons＜0.5%, total sulfur＜2ppm) fully.
Remaining TJ-2 regeneration: remaining TJ-2 is got kerosene 335ml with kerosene by 1: 1 volume ratio mix with it, add thermal distillation; Slowly be heated to 110～120 ℃, constant temperature 2 hours steams TJ-2, continues to be warmed up to 190～200 ℃, and constant temperature 30min stops distillation; Overhead product obtains regeneration TJ-2 extraction agent through condensation recovery, settlement separate, and distillation residue are the diesel cetane-number improver product of making solvent with kerosene.
The processing of remaining TJ-1 and remaining aluminum chloride: the about 20ml of water that slowly adds 5 times of quality in remaining aluminum chloride is hydrolyzed, and the hydrogen chloride gas water that hydrolysis produces absorbs, and promptly obtains technical hydrochloric acid (30%) 7.5g.Remaining TJ-1 is heated to 90～120 ℃ of distillations reclaims nitric acid and be used to prepare TJ-1, the residuum after the distillation adds gradually in the hydrolyzed solution of aluminum chloride resistates and mixes, and obtains the oil-aqeous suspension 33ml of sulfur acid aluminium salt; Leave standstill the suspension phase-splitting, on be the residual raw materials oil of recovery mutually, as the cetane number improver solvent, filter phase down, filter residue and filtrate, filter residue is the cetane number improver of recovery, filtrate is then removed synthesized polymer Tai-Ace S 150.
Through the aforesaid operations step, every processing 100g stock oil can obtain aluminum foil rolling oil 92.8g, cetane number improver 9.2g, technical hydrochloric acid (30%) 7.5g, polyaluminium sulfate 75g (salic 10～12.5%).
Embodiment 2: get 68% nitric acid 6g, 98% sulfuric acid 5g, at room temperature slowly mix, promptly obtain 11g and take off fragrant agent TJ-1; Get low mass molecule alcohol 80ml (wherein methyl alcohol 10ml, ethanol 50ml or Virahol 20ml), organic bases 320ml (wherein quadrol 50ml, diethylamine 200ml, propylene diamine 70m1), press alcohol/alkali (volume ratio)=mixing in 20: 80, promptly get 400ml extraction agent TJ-2.Ratio in TJ-1/ stock oil (mass ratio)=0.10, get and take off fragrant agent 10g and add gradually under room temperature by the containing among aromatic hydrocarbons 4.69%, total sulfur 452ppm 30～90 ℃ the straight run oil 100g of crude production in the river, all the other steps press example 1 described method and are operated.Every processing 100g stock oil can obtain soybean extracting solvent no.6 94g, does not contain aromatic hydrocarbon and sulfide fully, satisfy quality index: no aromatic hydrocarbon, sulfide＜0.05%, cetane number improver 7.1g, technical hydrochloric acid (30%) 6.9g, polyaluminium sulfate 70g (salic 10～12.5%).
Embodiment 3: get 68% nitric acid 9.5g, 98% sulfuric acid 5.5g, at room temperature slowly mix, promptly obtain 15g and take off fragrant agent TJ-1; Get low mass molecule alcohol 120ml (wherein methyl alcohol 40ml, ethanol 20ml or Virahol 60ml), organic bases 280ml (wherein propylene diamine 100ml, triethylamine 55ml, dipropyl amine 95ml, Diisopropylamine 30ml), press alcohol/alkali (volume ratio)=mixing in 30: 70, promptly get 400ml extraction agent TJ-2.Ratio in TJ-1/ stock oil (mass ratio) 0.12, get and take off fragrant agent 12g and add gradually among 170～270 ℃ of straight run kerosene 100g (constant temperature is 50～60 ℃) that contain aromatic hydrocarbons 7.13%, total sulfur 970ppm that produced by gas ore deposit in the river, all the other steps press example 1 described method and are operated.Every processing 100g stock oil, can obtain not have aromatic hydrocarbons kerosene (odorless kerosene(OK)) 90g (complete aromatic free and sulfide, satisfy quality index: aromatic hydrocarbon＜1%, sulfide＜5ppm), cetane number improver 11.6g, technical hydrochloric acid (30%) 7.4g, polyaluminium sulfate 73g (salic 10～12.5%).
Embodiment 4: take off fragrant agent TJ-1, extraction agent TJ-2 by example 3 described method preparations.In the ratio of TJ-1/ stock oil (mass ratio)=0.11, at room temperature to get and take off fragrant agent 11g and add gradually among 60～70 ℃ of straight runs oil 100g that contain aromatic hydrocarbons 3.62%, total sulfur 30ppm by crude production in the river, all the other steps press example 1 described method and are operated.Every processing 100g stock oil can obtain perfume extraction solvent 94g and (not contain aromatic hydrocarbon and sulfide fully, satisfy quality index: no aromatic hydrocarbon, sulfide＜0.05%), cetane number improver 6.9g, technical hydrochloric acid (30%) 6.5g, polyaluminium sulfate 70g (salic 10～12.5%).
Claims (7)
1. the method for a removing sulfur and arene from solvent oil, be to adopt nitrated-extraction-absorption method to produce solvent oil, it is characterized in that: nitric acid with 68% and 98% sulfuric acid, pressing nitric acid at room temperature mixes with vitriolic mass ratio 1.2～1.7: 1, promptly obtain taking off fragrant agent TJ-1, TJ-1 and stock oil are added constant temperature in 50～60 ℃ stock oil gradually in the ratio of mass ratio 0.10～0.12, stirring reaction 25～35min, aromatic hydrocarbons in the stock oil is converted into itrated compound, this itrated compound is a kind of diesel oil octane promoter, the neutral sulfide in the stock oil is relaxed be oxidized to polarity sulfide; Use 3 kinds of C then
1～C
3The arbitrary proportion mixture of the arbitrary proportion mixture of low mass molecule alcohol and at least 3 kinds of organic basess that are selected from quadrol, diethylamine, propylene diamine, triethylamine, dipropyl amine and Diisopropylamine by volume 30～20: 70～80 mix, promptly obtain extraction agent TJ-2, with nitrated stock oil and extraction agent TJ-2 is 1～1/2 by volume, in normal pressure and room temperature～50 ℃ mixing down, aromatic hydrocarbon itrated compound and polarity sulfide are extracted from nitrated stock oil; With residual aromatics and itrated compound thereof in the stock oil of sorbent material aluminum trichloride (anhydrous) adsorbing and removing extraction and whole organosulfur, promptly obtain the solvent oil product at last.
2. method according to claim 1, it is characterized in that: after TJ-1 and stock oil hybrid reaction, reaction mixture sat 3～8min, nitrated stock oil and remaining TJ-1 promptly are separated, nitrated stock oil is sent to extraction, and remaining TJ-1 then removes to reclaim nitric acid and preparation polyaluminium sulfate.
3. method according to claim 1, it is characterized in that: nitrated stock oil is mixed with extraction agent TJ-2, extraction 3～5min, to extract mixture and leave standstill 5～10min, the stock oil and the remaining TJ-2 of extraction promptly are separated, reclaim remaining TJ-2, get fresh TJ-2 again the stock oil that extracts is extracted next time, extraction times is 3～5 times.
4. method according to claim 1, it is characterized in that: with the stock oil of sorbent material aluminum trichloride (anhydrous) and extraction, ratio in mass ratio 0.0267 takes by weighing aluminum trichloride (anhydrous), milling, the back is rapid to add in the stock oil that extracts, airtight, 90 ℃ of constant temperature, settlement separate 20min behind the stirring 30min, the Filtration Adsorption mixture promptly obtains the solvent oil product; The sorbent material resistates is used to reclaim cetane number improver.
5. method according to claim 3 is characterized in that: the remaining TJ-2 that will reclaim mixed with kerosene in 1: 1 by volume, slowly was heated to 110～120 ℃, constant temperature 2 hours steams extraction agent TJ-2, continues to be warmed up to 190～200 ℃, constant temperature 30min stops distillation; Overhead product reclaims through condensation, obtains regenerating extracting agent TJ-2, and distillation residue are the diesel cetane-number improver product that is dissolved in kerosene or diesel oil solvent.
6. method according to claim 2, it is characterized in that: with the stock oil of sorbent material aluminum trichloride (anhydrous) and extraction, ratio in mass ratio 0.0267 takes by weighing aluminum trichloride (anhydrous), milling, the back is rapid to add in the stock oil that extracts, airtight, 90 ℃ of constant temperature, settlement separate 20min behind the stirring 30min, the Filtration Adsorption mixture promptly obtains the solvent oil product; The sorbent material resistates is used to reclaim cetane number improver.
7. method according to claim 6 is characterized in that: the water that slowly adds 5 times of quality in the sorbent material resistates is hydrolyzed, and the hydrogen chloride gas water that hydrolysis produces absorbs, and promptly obtains technical hydrochloric acid; Remaining TJ-1 is heated to 90～120 ℃, and distillation recovery nitric acid is used for preparation and takes off fragrant agent TJ-1; Residuum after the distillation adds gradually in the hydrolyzed solution of sorbent material aluminum chloride resistates and neutralizes, and obtains the oil solution suspension of sulfur acid aluminium salt; Leave standstill the suspension phase-splitting, on be the residual raw materials oil of recovery mutually, described residual raw materials oil is as the cetane number improver solvent, filter down mutually filter residue and filtrate, filter residue is the cetane number improver of recovery, filtrate is then removed synthesized polymer Tai-Ace S 150.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 01108455 CN1227330C (en) | 2001-05-23 | 2001-05-23 | Process for removing sulfur and arene from solvent oil |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 01108455 CN1227330C (en) | 2001-05-23 | 2001-05-23 | Process for removing sulfur and arene from solvent oil |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1386823A CN1386823A (en) | 2002-12-25 |
| CN1227330C true CN1227330C (en) | 2005-11-16 |
Family
ID=4657272
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 01108455 Expired - Fee Related CN1227330C (en) | 2001-05-23 | 2001-05-23 | Process for removing sulfur and arene from solvent oil |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1227330C (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100404646C (en) * | 2005-02-05 | 2008-07-23 | 中国石油化工股份有限公司 | Method for modifying poor-quality diesel-oil by cut fraction |
| CN101967391A (en) * | 2010-09-30 | 2011-02-09 | 西南石油大学 | Complex sulfurization and denitrification method for distillate |
| CN108117888B (en) * | 2016-11-28 | 2020-06-23 | 中国科学院大连化学物理研究所 | Method for desulfurizing hydrogenated fuel oil |
-
2001
- 2001-05-23 CN CN 01108455 patent/CN1227330C/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| CN1386823A (en) | 2002-12-25 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN1257254C (en) | Process for removing low amounts of organic sulfur from hydrocarbon fuels | |
| US7244352B2 (en) | Selective hydroprocessing and mercaptan removal | |
| CN113195687A (en) | Solvent for aromatic extraction process | |
| Haruna et al. | Sulfur removal technologies from fuel oil for safe and sustainable environment | |
| CN101376842B (en) | Method for reducing sulfur content in gasoline | |
| Aitani et al. | A review of non-conventional methods for the desulfurization of residual fuel oil | |
| CN102021010A (en) | Processing method of middle and low temperature coal tar | |
| CN105176570B (en) | A kind of method of the desulfurization by oxidation and extraction based on ionic liquid | |
| CN1227330C (en) | Process for removing sulfur and arene from solvent oil | |
| US20050218038A1 (en) | Pre-treatment of hydrocarbon feed prior to oxidative desulfurization | |
| CN1235843C (en) | Method for eliminating and reclaiming acid component from oil products | |
| RU2203306C2 (en) | Method of preparing feedstock for catalytic cracking and hydrocracking | |
| CN101343554A (en) | Process for preparing light-end product | |
| Huseynov | Selective purification of transformer oil by the method of ionic liquid extractive purification | |
| CN1342630A (en) | Process for preparing high-purity n-pentane | |
| CN102876361B (en) | A kind of coupling method of petroleum naphtha Porous deproteinized bone-vehicle fuel oil desulfurization | |
| RU2514916C9 (en) | Method for production of commercial-grade diesel fuel of high-sulphur diesel oil cuts and device for its implementation | |
| CN1335353A (en) | Comprehensive acid sludge and caustic sludge treating process | |
| CN1313572C (en) | Low sulfur, low arene aluminum board hammering base oil preparation method | |
| US2671047A (en) | Refining hydrocarbon materials with so2 and bf3 | |
| US2727851A (en) | Refining of heater oil | |
| RU2429276C2 (en) | Diesel fraction purification method | |
| KR100524447B1 (en) | Method for preparing natural hetero compound and use thereof | |
| CN102040553A (en) | Preparation method of gasoline extraction and desulfurization agent | |
| Lazorko et al. | Investigation of straight-run diesel oil fractions with sulphur high content oxidative desulphurization |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| ASS | Succession or assignment of patent right |
Owner name: SOUTHWEST PETROLEUM INSTITUTE Free format text: FORMER OWNER: SOUTHWEST PETROLEUM INSTITUTE; NANTONG JIALING PETROCHEMICAL TECHNOLOGY DEVELOPMENT CENTER Effective date: 20030730 |
|
| C41 | Transfer of patent application or patent right or utility model | ||
| TA01 | Transfer of patent application right |
Effective date of registration: 20030730 Applicant after: South-west Petroleum College Applicant before: South-west Petroleum College Applicant before: Nanchong Jialing Petrochemical Technology Development Center |
|
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C19 | Lapse of patent right due to non-payment of the annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |