CN102041089A - Hydrotreating method for producing low-sulphur and ultra-low sulphur diesel oil - Google Patents
Hydrotreating method for producing low-sulphur and ultra-low sulphur diesel oil Download PDFInfo
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Abstract
The invention provides a hydrotreating method for producing low-sulphur and ultra-low sulphur diesel oil, which comprises the following steps of: subjecting raw oil into pre-hydrogenation reaction in the first reaction region, then fractionating the diesel oil into a light fraction and a heavy fraction after implementing pre-hydrogenation, and then absorbing or extracting the heavy fraction to remove the organic nitrogen-containing compound which has an inhibition effect to deep desulfurization; infusing the heavy fraction into the second reaction region to implement deep hydrodesulfurization after removing the organic nitrogen-containing compound; and mixing the light fraction and the heavy fraction to obtain producing low-sulphur or ultra-low sulphur diesel oil. Compared with conventional refining process of diesel oil, the hydrotreating method for producing low-sulphur and ultra-low sulphur diesel oil provided by the invention has the advantages that the purpose for deep or ultra-deep hydrodesulfurization of diesel oil can be realized in the condition that the whole operation conditions are relatively mild due to the point that the negative factor which can influence the deep hydrodesulfurization of diesel oil is removed, and the hydrogen consumption of the method is relatively low.
Description
Technical field
The present invention relates to a kind of hydroprocessing process of producing low-sulfur and ultra-low-sulphur diesel, belong to the petrochemical technology field.
Background technology
Along with the development of world economy, various countries are also increasing day by day to the demand of the energy.In the present available energy structure, based on the energy development of oil with utilize and still be in dominant position.Since the eighties in last century, countries in the world have been ascendant trend gradually to the demand of diesel oil.Scholarly forecast 2005 to 2010, China is that 6.6%, 2010 year China's diesel oil demand is estimated to reach 1.2 hundred million tons to diesel oil demand average growth rate per annum.
Because petroleum resources deficient day by day and to the continuous growth of diesel oil demand in the world wide, it is increasing to derive from the shared share of the diesel oil of heavy oil cracking, causes containing in the diesel oil distillate heteroatoms and aromatic hydrocarbon such as a large amount of sulphur, nitrogen.The discharge that forms behind these substance combustions is serious all the more to the pollution of environment, causes the common concern of countries in the world gradually.For example, the regulation sulphur content rose and to begin to carry out Europe IV standard less than 350 μ g/g in 2005 in the Europe III diesel oil standard that European Union in 2000 implements, and the sulphur content in the derv fuel oil is less than 50 μ g/g.In the world fuel standard derv fuel oil sulphur content is also had strict more restriction, the sulphur content of diesel oil requires less than 300 μ g/g in its II class standard, and III class and IV class standard then require the diesel oil sulphur content less than 30 μ g/g and 10 μ g/g respectively.The diesel oil standard of China is also positive to walk with world's pace at a quick pace.Beijing, Shanghai, three big cities, Guangzhou take the lead in proposing to reach the EUROIII Emission Standard requirement derv fuel oil quality product in 2005, reach the requirement of Europe IV standard in 2008.
Sulfide in the diesel oil distillate mainly contains mercaptan, thioether, disulphide, thiophene-based, benzothiophene kind (BTs), dibenzothiophene class (DBTs) etc.Studies show that (Sinopec press published " hydrofining " P32-P33 in 2006), the diesel oil that contains the above-mentioned type sulfide total 1.0% is carried out hydrogenation, the refined diesel oil sulphur content is 0.24% o'clock, when promptly controlling desulfurization degree and be 76.0% refining depth, non-thiophene-type sulfide in the diesel oil all disappears, and the simple relatively thiophene of structure and thionaphthene also are removed in the thiophene-based.Have only dibenzothiophene and more complicated thiophene sulfocompounds still to be retained in the diesel oil; Continue to improve refining depth, the sulphur content of hydrogenated diesel oil is 0.11% o'clock, and both having controlled desulfurization degree is 89.0%, and dibenzothiophene disappears, 4-MDBT and 4, and the 6-dimethyl Dibenzothiophene still exists, and just the former content obviously reduces; When the hydrogenated diesel oil sulphur content had only 0.018%, promptly controlling desulfurization degree was 98.2%, and 4-MDBT just is removed, and 4, the 6-dimethyl Dibenzothiophene still obviously exists; When sulphur content in the hydrogenated diesel oil is 0.005%, 4, the 6-dimethyl Dibenzothiophene reduces to some extent, but still obviously exists.Therefore, desire to expect the diesel oil of sulphur content less than 50 μ g/g, alkyl diphenyl thiophthene class also must remove.
Influence respond hydrogen sulfide content in the content of organic compounds containing nitrogen in the thing and recycle hydrogen, the stock oil of principal element that dibenzothiophene and alkyl diphenyl thiophthene class sulfide removes.Isoda (Hydrodesulfurization of refractory sulfur species " Energy ﹠amp; Fuel " 1996,10 (2): 482-486) wait the people to discover, 4-MDBT and 4, the 6-DMDBT desulphurization reaction is mainly undertaken by the hydrogenation path.According to denitrification reaction mechanism, what the C-N bond rupture on the aromatic ring must be through aromatic hydrocarbons is saturated, thus organic compounds containing nitrogen can with dibenzothiophene, alkyl diphenyl thiophthene competitive adsorption on identical hydrogenation activity position, influence the effect of desulfurization.Therefore, the content of organic compounds containing nitrogen helps producing ultra-low-sulphur diesel in the reduction raw material.Hydrogen sulfide influences Ultra-deep Desulfurization of Diesel Fuels and mainly contains two aspect factors, is that the molecular ratio of hydrogen sulfide is less on the one hand, and adsorptive power is better than dibenzothiophene and alkyl diphenyl thiophthene sulfide on the activity of such catalysts position.People such as Kabe (Effects of H2S on hydrodesulfurization of dibenzothiophene and 4,6-dimethyldibenzothiophene on alumina-supported NiMo nd NiW catalysts " Applied catalysis " A.general, 2001,209 (1/2): 237) measured MDBT, DMDBT, H
2The heat of adsorption of S on catalyzer, it is MDBT＜DMDBT＜H in proper order
2S.Along with the rising of temperature of reaction, H
2The absorption constant of S on catalyzer descends, and its restraining effect can weaken; On the other hand, because the hydrogen sulfide in the recycle hydrogen increases, the hydrogen dividing potential drop then descends, and influences hydrogenation reaction and carries out to positive dirction, thereby cause deep desulfuration or ultra-deep desulfurization more harsh.
In full fraction deep of diesel oil or ultra-deep hydrodesulfuration process, need saturated a large amount of aromatic hydrocarbons in order to remove a spot of sulphur, must pay huge cost of investment and process cost.For example, the processing sulphur content is 1.31%～2.24% raw material, and the production sulphur content is compared less than 500 μ g/g diesel oil with the production sulphur content less than 50 μ g/g diesel oil, and the hydrogen pressure that is increased and hydrogen consumption will be greater than 1 times, even up to 3 times.(aromatic hydrocarbons " oil refining design ", the 32nd the 2nd phase of volume are taken off in the hydrogenating desulfurization of diesel oil distillate)
The organic compounds containing nitrogen that extraction process or absorption method remove in the diesel oil is common non-hydrogen denitrogenation method, and the general extraction agent or the sorbent material that suit of adopting removes the nitrogenous compound in the diesel raw material, and the yield that its main weak point is diesel oil is lower slightly.U.S. Pat 6551501 has been described diesel oil before hydrotreatment, removes the inhibitor that influences hydrogenating desulfurization earlier and contains the N compound, carries out diesel hydrogenation for removal sulphur afterwards again.This technology can improve the degree of depth of hydrogenating desulfurization, but the full cut of diesel oil adopts methods such as absorption, extraction to remove to be contained the N compound and can cause diesel yield to descend a lot.
Chinese patent CN1483069A has set forth a kind of method of gas oil hydrogenating desulfurization.This process mainly be with diesel oil be fractionated into light, weigh two components, light constituent carries out hydrogenation reaction under lower hydrogen-oil ratio condition, heavy constituent are carried out hydrogenation reaction under higher hydrogen-oil ratio condition, the hydrogen behind the heavy constituent hydrogenation need not to handle, and can continue on for the hydrogenation of light constituent diesel oil.This method is not considered the influence to deep hydrodesulfurizationof of diesel oil of N compound and hydrogen sulfide, and air speed is lower.
Summary of the invention
At the deficiencies in the prior art, the invention provides a kind of new diesel oil hydrotreating method.The inventive method can reduce equipment cost and process cost and obtain the super low sulfur product.
The hydroprocessing process that the present invention produces low-sulfur and ultra-low-sulphur diesel comprises following content: at first carry out the pre-hydrotreatment of diesel oil under the demulcent condition, sulphur in the diesel oil is taken off to 500 μ g/g or below the 350 μ g/g, and sulfocompound is mainly dibenzothiophene and alkyl diphenyl thiophthene in the raw material at this moment.Because the boiling point of dibenzothiophene and alkyl diphenyl thiophthene higher (seeing Table 1), so with the diesel oil behind the pre-hydrogenation be divided into light, weigh two components, light constituent is super low sulfur or does not have the sulfur diesel component that heavy constituent remove the inhibitor organic compounds containing nitrogen through processes such as extraction or absorption.Deep hydrodesulfurizationof is carried out in the heavy constituent that remove the inhibitor organic compounds containing nitrogen, obtains the heavy constituent diesel oil of low-sulfur or super low sulfur.At last light, heavy constituent are mixed, obtain low-sulfur or ultra-low-sulphur diesel.
The treatment process of a kind of low-sulfur of the present invention or ultra-low-sulphur diesel hydrogenation comprises following content:
A, stock oil at first enter the pre-hydrogenation of first reaction zone, carry out preliminary hydrogenating desulfurization, denitrogenation and aromatic hydrocarbons saturated reaction;
The diesel oil of b, the pre-hydrogenation of process step a enters fractionation plant, is separated into light constituent diesel oil and heavy constituent diesel oil;
The isolated heavy constituent diesel oil of c, step b enters and removes the organic compounds containing nitrogen device, removes the organic compounds containing nitrogen that influences the degree of depth or ultra-deep hydrodesulfuration;
D, the heavy constituent diesel oil that removes organic compounds containing nitrogen through step c carry out the degree of depth or ultra-deep hydrodesulfuration at second reaction zone, mix with the isolated light constituent diesel oil of step b then.
The pre-hydrogenation process of described first reaction zone of step a can be taken off sulphur to 500 μ g/g or below the 350 μ g/g.The first reaction zone pre-hydrogenator can adopt existing reaction formations such as fixed bed, fluidized-bed, ebullated bed or moving-bed, and its working pressure is 2.0～5.0MPa, is preferably 3.0～4.5MPa; Volume space velocity is 2.0～5.0h during liquid
-1, be preferably 3.0～4.0h
-1Temperature of reaction is controlled at 280～360 ℃, is preferably 320～350 ℃; Hydrogen to oil volume ratio is 150: 1～450: 1, is preferably 200: 1～350: 1.
In step b diesel oil fractionation process, the cut point of light constituent diesel oil and heavy constituent diesel oil is controlled at 280～350 ℃, is preferably 300～340 ℃.
Step c removes the organic compounds containing nitrogen part can adopt extraction process or absorption method etc.When adopting extracting process, solvent can be selected a kind of independent use or several compound use of low-carbon alcohol (methyl alcohol, ethanol), acetone, furfural, phenol, dimethyl sulfoxide (DMSO), dimethyl formamide etc.The salt (iron(ic) chloride, aluminum chloride, cupric chloride, cobalt chloride, Manganous chloride tetrahydrate, zinc chloride and Cadmium chloride fine powder etc.) or the mineral acid that also can be aided with transition metal ion simultaneously extract; When adopting adsorption method, sorbent material adopts one or more in gac, silicon-dioxide, aluminum oxide, catalytic cracking poiser, molecular sieve, the resin etc.According to practical situation, each sorbent material can carry out modification in advance to be handled.No matter adopt which kind of method, diesel yield is not less than 96%, and the total nitrogen decreasing ratio is not less than 70%, and basic nitrogen removal rate is not less than 85% (all the weight with the diesel oil heavy constituent is benchmark).Extraction removes the concrete operation method of organic compounds containing nitrogen or adsorbing and removing organic compounds containing nitrogen and can determine by the existing knowledge in this area.
Carry out the reaction of the degree of depth or ultra-deep hydrodesulfuration and adopt operating method such as the downward trickle bed of gas and liquid flowing, gas-liquid counter current, the liquid-phase hydrogenatin of liquid product round-robin in described second reaction zone of steps d, concrete operations mode and operational condition can require to be determined by those skilled in the art according to feed properties and quality product.The deep hydrodesulfurizationof operation condition is generally: pressure is 3.4～10.0MPa, is preferably 5.0～8.0MPa; Volume space velocity is 1.0～3.0, is preferably 1.0～2.0h
-1Temperature of reaction is controlled at 280～370 ℃, is preferably 330～360 ℃; Hydrogen to oil volume ratio is 100: 1～1000: 1, is preferably 150: 1～800: 1.When adopting liquid product round-robin liquid-phase hydrogenatin mode, do not use the recycle hydrogen system, hydrogen is dissolved in the liquid phase, circulation volume ratio (internal circulating load and fresh feed amount volume ratio) was generally preferred 1: 1～5: 1 0.5: 1～10: 1.
Identical hydrogenation catalyst can be used in described two reaction zones of step a, d, also different Hydrobon catalysts can be used.The active higher hydrogenation catalyst of the preferred direct desulfurization of first reaction zone, as contain the hydrogenation catalyst etc. of Mo-Co, Mo-Co-Ni; The hydrogenation catalyst that the preferred hydrodesulfurization activity of second reaction zone is higher, as contain the hydrogenation catalyst etc. of Mo-Ni, W-Ni, W-Mo-Ni or W-Mo-Co-Ni, catalyzer can adopt the commercial goods catalyzer by root, also can prepare according to this area ordinary method.According to the raw material specific nature, each reactor zone can be independent a kind of catalyzer, also can several catalyst mix or grating use.
The raw material that the present invention handles is any hydrocarbon raw material of boiling range in 130～380 ℃ of scopes.Generally include one or more mixing of spray vapour fuel, straight-run diesel oil, coker gas oil, catalytic diesel oil etc.
Compare with traditional diesel refining treatment process, technology of the present invention can relatively realize diesel oil deep or ultra-deep hydrodesulfuration under the demulcent operational condition in integral body, and the hydrogen consumption is lower, specifically has following advantage:
1, higher according to the boiling point of alkyl diphenyl thiophthene class, the diesel oil behind the pre-hydrogenation can be carried out gently, heavily separate.Heavy constituent enter the deep desulfuration reactor after removing organic compounds containing nitrogen, adopt the operating method of vapour-liquid adverse current to carry out the degree of depth or ultra-deep hydrodesulfuration.Owing to got rid of the unfavorable factor that influences deep desulfuration or ultra-deep desulfurization, deep desulfuration or the ultra-deep desulfurization of realizing diesel oil under the demulcent condition can compared.
2, the diesel oil behind the pre-hydrogenation mainly contains dibenzothiophene class and alkyl diphenyl thiophthene class sulfide, is distributed in the heavy constituent, and the ratio that heavy constituent account for raw material is 20v%～50v%, so the treatment capacity of second reaction zone is less, can use less reactor.With respect to traditional diesel refining technology, overall air speed is higher.
3, contain sulfide hardly in the light constituent of diesel oil behind the pre-hydrogenation, need not further processing.Avoid deep hydrogenation to cause a large amount of aromatic hydrocarbons saturated, can reduce the reactive hydrogen consumption, improved diesel yield.
4, because denitrogenation, hydrofining are carried out in the diesel oil heavy constituent targetedly, do higher diesel oil distillate raw material so can process.
Description of drawings
Fig. 1 is the treatment process process flow diagram of low-sulfur of the present invention or ultra-low-sulphur diesel hydrogenation.
Embodiment
Be explanation the solution of the present invention and effect, further specify feature of the present invention by following examples:
Feedstock property sees Table 2
Embodiment 1
Present embodiment first reaction zone adopts Mo-Co type Hydrobon catalyst (the FDS-4 Hydrobon catalysts of Fushun Petrochemical Research Institute's development and production), the direct hydrodesulfurization activity of this catalyzer is higher, second reaction zone adopts W-Mo-Ni-Co type Hydrobon catalyst (the FH-UDS Hydrobon catalysts of Fushun Petrochemical Research Institute's development and production), and this catalyzer has denitrogenation, aromatic hydrocarbons is saturated and the active high characteristics of deep hydrodesulfurizationof.Diesel oil behind the pre-hydrogenation of first reaction zone is divided into＜340 ℃ of lighting ends and＞340 ℃ of last running,＞340 ℃ of last running are sent into second reaction zone after the absorption denitrogenation, and second reaction zone adopts the downward operating method of gas and liquid flowing.Adopt acidic cationic resin absorption denitrogenation, diesel yield 99.5%, total nitrogen decreasing ratio 78%.Other processing condition and treated oil product property see Table 3.
Embodiment 2
Present embodiment first reaction zone adopts Mo-Co type Hydrobon catalyst (the FDS-4 Hydrobon catalysts of Fushun Petrochemical Research Institute's development and production), the direct hydrodesulfurization activity of this catalyzer is higher, second reaction zone adopts W-Mo-Ni type Hydrobon catalyst (the FH-98 Hydrobon catalysts of Fushun Petrochemical Research Institute's development and production), and this catalyzer has denitrogenation, aromatic hydrocarbons is saturated and the active high characteristics of deep hydrodesulfurizationof.Diesel oil behind the pre-hydrogenation of first reaction zone is divided into＜300 ℃ of lighting ends and＞300 ℃ of last running,＞300 ℃ of last running are sent into second reaction zone after the absorption denitrogenation, and second reaction zone adopts the gas-liquid counter current operating method.Adopt dimethyl sulfoxide (DMSO) extraction denitrogenation, diesel yield 98.7%, total nitrogen decreasing ratio 67%.Other processing condition are seen and the treated oil product property sees Table 3.
Comparative example
Present embodiment adopts traditional conventional hydrofining technology, and diesel raw material is directly through two hydrofining reaction districts.First reaction zone adopts Mo-Co type Hydrobon catalyst (the FDS-4 Hydrobon catalysts of Fushun Petrochemical Research Institute's development and production), the direct hydrodesulfurization activity of this catalyzer is higher, second reaction zone adopts W-Mo-Ni-Co type Hydrobon catalyst (the FH-UDS Hydrobon catalysts of Fushun Petrochemical Research Institute's development and production), this catalyzer has denitrogenation, aromatic hydrocarbons is saturated and the active high characteristics of deep hydrodesulfurizationof, processing condition and the results are shown in Table 4, other is identical with embodiment 1.From the data of embodiment 1 and comparative example as can be seen, under close processing condition, the present invention program can obtain higher desulfurization degree.Simultaneously, the present invention program have also that hydrogen consumption is low, process cost and advantages such as the facility investment expense is low, flexible operation.
Main sulfocompound in table 1 diesel oil distillate
| Reactant | Relative reaction rate | Boiling point, ℃ |
| Thiophene | 100 | 90 |
| Thionaphthene | 30 | 237 |
| Dibenzothiophene | 30 | 333 |
| Methyldibenzothiophene | 5 | 339～351 |
| Dimethyl Dibenzothiophene | 1 | 357～369 |
| The trimethylammonium dibenzothiophene | 1 | 370～387 |
Table 2 stock oil character
Table 3 embodiment hydrofining technology condition and result
Table 4 comparative example hydrofining technology condition and result
Claims (10)
1. hydroprocessing process of producing low-sulfur and ultra-low-sulphur diesel comprises following process:
A, stock oil at first enter the pre-hydrogenation of first reaction zone, carry out preliminary hydrogenating desulfurization, denitrogenation and aromatic hydrocarbons saturated reaction;
The diesel oil of b, the pre-hydrogenation of process step a enters fractionation plant, is separated into light constituent diesel oil and heavy constituent diesel oil;
The isolated heavy constituent diesel oil of c, step b enters and removes the organic compounds containing nitrogen device, removes the organic compounds containing nitrogen that influences the degree of depth or ultra-deep hydrodesulfuration;
D, the heavy constituent diesel oil that removes organic compounds containing nitrogen through step c carry out the degree of depth or ultra-deep hydrodesulfuration at second reaction zone, mix with the isolated light constituent diesel oil of step b then.
2. it is characterized in that in accordance with the method for claim 1: the pre-hydrogenation process of described first reaction zone of step a takes off sulphur to 500 μ g/g or below the 350 μ g/g.
3. according to claim 1 or 2 described methods, it is characterized in that: the first reaction zone pre-hydrogenator adopts fixed bed, fluidized-bed, ebullated bed or moving bed reaction form, and its working pressure is 2.0～5.0MPa, and volume space velocity is 2.0～5.0h during liquid
-1, temperature of reaction is controlled at 280～360 ℃, and hydrogen to oil volume ratio is 150: 1～450: 1.
4. according to claim 1 or 2 described methods, it is characterized in that: the first reaction zone pre-hydrotreating reaction working pressure is 3.0～4.5MPa, and volume space velocity is 3.0～4.0h during liquid
-1, temperature of reaction is controlled to be 320～350 ℃, and hydrogen to oil volume ratio is 200: 1～350: 1.
5. in accordance with the method for claim 1, it is characterized in that: in step b diesel oil fractionation process, the cut point of light constituent diesel oil and heavy constituent diesel oil is controlled at 280～350 ℃.
6. according to claim 1 or 5 described methods, it is characterized in that: in the step b diesel oil fractionation process, the cut point of light constituent diesel oil and heavy constituent diesel oil is controlled to be 300～340 ℃.
7. in accordance with the method for claim 1, it is characterized in that: step c removes organic compounds containing nitrogen and adopts extraction process or absorption method, and the total nitrogen decreasing ratio is not less than 70%.
8. it is characterized in that in accordance with the method for claim 7: the solvent that extraction process removes organic compounds containing nitrogen is selected a kind of independent use or several compound use in methyl alcohol, ethanol, acetone, furfural, phenol, dimethyl sulfoxide (DMSO) and the dimethyl formamide; The sorbent material that absorption method removes organic compounds containing nitrogen is one or more in gac, silicon-dioxide, aluminum oxide, catalytic cracking poiser, molecular sieve or the resin.
9. it is characterized in that in accordance with the method for claim 1: carry out the degree of depth or downward trickle bed, gas-liquid counter current, the liquid product round-robin liquid-phase hydrogenatin operating method of ultra-deep hydrodesulfuration reaction employing gas and liquid flowing in rapid described second reaction zone of d.
10. it is characterized in that in accordance with the method for claim 1: first reaction zone uses the hydrogenation catalyst that contains Mo-Co, Mo-Co-Ni; Second reaction zone uses and contains Mo-Ni, W-Ni, W-Mo-Ni or W-Mo-Co-Ni hydrogenation catalyst.
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN102876367A (en) * | 2011-07-11 | 2013-01-16 | 中国石油化工股份有限公司 | Deep desulphurization dearomatization combination method of diesel oil |
| CN103059978A (en) * | 2011-10-21 | 2013-04-24 | 中国石油化工股份有限公司 | Single-stage series diesel oil hydrofining method |
| CN103102943A (en) * | 2011-11-10 | 2013-05-15 | 中国石油化工股份有限公司 | Treating method for in-depth desulphurization and dearomatization of diesel oil fraction |
| CN103740406A (en) * | 2014-01-21 | 2014-04-23 | 湖北金鹤化工有限公司 | Extraction-hydrogenation combined process for producing low-sulfur-content gasoline |
| CN105132016A (en) * | 2015-09-29 | 2015-12-09 | 肖军 | Ultrasonic-assisted vehicle-use fuel linkage desulfurization system complete equipment and desulfurization method |
| CN110655954A (en) * | 2018-06-28 | 2020-01-07 | 中国石油化工股份有限公司 | Ultra-deep desulfurization method for residual oil hydrogenated diesel oil |
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| CN1483069A (en) * | 2000-11-17 | 2004-03-17 | ���ջ�����ʽ���� | Method of desulfurizing gas oil fraction, desulfurized gas oil, and desulfurizer for gas oil fraction |
| CN101120075A (en) * | 2005-02-17 | 2008-02-06 | Sk能源株式会社 | Process for producing ultra low sulfur and low aromatic diesel fuel |
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| EP1057879A2 (en) * | 1999-06-02 | 2000-12-06 | Haldor Topsoe A/S | A combined process for improved hydrotreating of diesel fuels |
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Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102876367A (en) * | 2011-07-11 | 2013-01-16 | 中国石油化工股份有限公司 | Deep desulphurization dearomatization combination method of diesel oil |
| CN102876367B (en) * | 2011-07-11 | 2015-04-15 | 中国石油化工股份有限公司 | Deep desulphurization dearomatization combination method of diesel oil |
| CN103059978A (en) * | 2011-10-21 | 2013-04-24 | 中国石油化工股份有限公司 | Single-stage series diesel oil hydrofining method |
| CN103059978B (en) * | 2011-10-21 | 2015-02-18 | 中国石油化工股份有限公司 | Single-stage series diesel oil hydrofining method |
| CN103102943A (en) * | 2011-11-10 | 2013-05-15 | 中国石油化工股份有限公司 | Treating method for in-depth desulphurization and dearomatization of diesel oil fraction |
| CN103102943B (en) * | 2011-11-10 | 2015-05-13 | 中国石油化工股份有限公司 | Treating method for in-depth desulphurization and dearomatization of diesel oil fraction |
| CN103740406A (en) * | 2014-01-21 | 2014-04-23 | 湖北金鹤化工有限公司 | Extraction-hydrogenation combined process for producing low-sulfur-content gasoline |
| CN105132016A (en) * | 2015-09-29 | 2015-12-09 | 肖军 | Ultrasonic-assisted vehicle-use fuel linkage desulfurization system complete equipment and desulfurization method |
| CN110655954A (en) * | 2018-06-28 | 2020-01-07 | 中国石油化工股份有限公司 | Ultra-deep desulfurization method for residual oil hydrogenated diesel oil |
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