CN101412928B - Hydro-desulphurizing combined method - Google Patents
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- CN101412928B CN101412928B CN 200810134134 CN200810134134A CN101412928B CN 101412928 B CN101412928 B CN 101412928B CN 200810134134 CN200810134134 CN 200810134134 CN 200810134134 A CN200810134134 A CN 200810134134A CN 101412928 B CN101412928 B CN 101412928B
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- 238000000034 method Methods 0.000 title claims abstract description 52
- 239000007789 gas Substances 0.000 claims abstract description 24
- 238000006243 chemical reaction Methods 0.000 claims abstract description 23
- 230000008569 process Effects 0.000 claims abstract description 22
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 21
- 239000001257 hydrogen Substances 0.000 claims abstract description 21
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 21
- 239000002994 raw material Substances 0.000 claims abstract description 19
- 239000007788 liquid Substances 0.000 claims abstract description 10
- 238000005194 fractionation Methods 0.000 claims abstract description 3
- 239000003054 catalyst Substances 0.000 claims description 21
- 239000002283 diesel fuel Substances 0.000 claims description 19
- 238000005984 hydrogenation reaction Methods 0.000 claims description 15
- 239000012071 phase Substances 0.000 claims description 14
- 229930195733 hydrocarbon Natural products 0.000 claims description 11
- 150000002430 hydrocarbons Chemical class 0.000 claims description 11
- 239000003502 gasoline Substances 0.000 claims description 8
- 239000007791 liquid phase Substances 0.000 claims description 6
- 239000004215 Carbon black (E152) Substances 0.000 claims description 5
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims description 4
- 230000003197 catalytic effect Effects 0.000 claims description 3
- 239000003245 coal Substances 0.000 claims description 3
- 239000011280 coal tar Substances 0.000 claims description 2
- 238000005516 engineering process Methods 0.000 abstract description 8
- 238000000926 separation method Methods 0.000 abstract description 7
- 238000004523 catalytic cracking Methods 0.000 abstract description 5
- 238000006477 desulfuration reaction Methods 0.000 abstract description 4
- 230000023556 desulfurization Effects 0.000 abstract description 4
- 230000010354 integration Effects 0.000 abstract 2
- 230000003009 desulfurizing effect Effects 0.000 abstract 1
- 239000003921 oil Substances 0.000 description 39
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 11
- 239000005864 Sulphur Substances 0.000 description 10
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 8
- 238000004519 manufacturing process Methods 0.000 description 5
- 238000009835 boiling Methods 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 239000000446 fuel Substances 0.000 description 4
- 229910052757 nitrogen Inorganic materials 0.000 description 4
- CIWBSHSKHKDKBQ-JLAZNSOCSA-N Ascorbic acid Chemical compound OC[C@H](O)[C@H]1OC(=O)C(O)=C1O CIWBSHSKHKDKBQ-JLAZNSOCSA-N 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 238000002360 preparation method Methods 0.000 description 3
- 238000007670 refining Methods 0.000 description 3
- 238000004939 coking Methods 0.000 description 2
- 150000001875 compounds Chemical class 0.000 description 2
- 230000007812 deficiency Effects 0.000 description 2
- 239000003208 petroleum Substances 0.000 description 2
- YZCKVEUIGOORGS-OUBTZVSYSA-N Deuterium Chemical compound [2H] YZCKVEUIGOORGS-OUBTZVSYSA-N 0.000 description 1
- 108010010803 Gelatin Proteins 0.000 description 1
- 239000008186 active pharmaceutical agent Substances 0.000 description 1
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 1
- 125000003118 aryl group Chemical group 0.000 description 1
- 238000000975 co-precipitation Methods 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 229920000159 gelatin Polymers 0.000 description 1
- 239000008273 gelatin Substances 0.000 description 1
- 235000019322 gelatine Nutrition 0.000 description 1
- 235000011852 gelatine desserts Nutrition 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- NLYAJNPCOHFWQQ-UHFFFAOYSA-N kaolin Chemical compound O.O.O=[Al]O[Si](=O)O[Si](=O)O[Al]=O NLYAJNPCOHFWQQ-UHFFFAOYSA-N 0.000 description 1
- 229910052622 kaolinite Inorganic materials 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 229910000510 noble metal Inorganic materials 0.000 description 1
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 239000003209 petroleum derivative Substances 0.000 description 1
- 238000005504 petroleum refining Methods 0.000 description 1
- 238000005554 pickling Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
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Abstract
The invention discloses a hydroprocessing and desulfurizing integration method, in particular a wax oil hydroprocessing and diesel hydrorefining integration process method. The method comprises the following steps: raw wax oil passes through a first reaction zone in the presence of hydrogen first, liquid obtained after separation of products is taken as catalytic cracking raw materia; hydrogen-containing gas and gas phase of light liquid obtained after separation are mixed with diesel raw material to enter a second reaction zone; and gas after separation of products in the second reaction zone is recycled after desulfurization, and liquid obtained after separation is subjected to fractionation to obtain hydrogenant naphtha and hydrogenant diesel. The method aims at technical characteristics of wax oil hydroprocessing and hydrorefining, integrates the two technologies for application, simplifies process flow, simplifies the process flow at the same time of meeting the same product requirements, and reduces equipment, investment and operating cost. The method is applied to newly built equipment to reduce equipment investment and applied to expanding reformation of the prior devices.
Description
Technical field
The present invention relates to a kind of hydro-desulphurizing combined method, particularly the comprehensive hydro-desulphurizing combined method of different boiling range hydrocarbon raw materials.
Background technology
Along with the sustainable development of world economy and the increasingly stringent of environmental regulation, need to produce a large amount of light clean fuels at present, these all require existing oil Refining Technologies is improved, and produce satisfactory product with minimum cost.Along with the worsening shortages of crude resources and heaviness, in poor quality development, catalytic cracking (FCC) and coking become the important means of production light Fuel product, but the quality product that these two kinds of techniques obtain generally is difficult to the finger figureofmerit requirement that reaches strict.In the light Fuel quality product system, sulphur content is most important index, how to reduce sulphur content in the petroleum products and be one of most significant problems that current refining of petroleum industry faces.At present, be applied widely in Clean Fuel Production take desulfurization as the main purpose hydrogenation technique.Such as the hydrogenation preconditioning technique of catalytically cracked material, light hydrocarbons (such as diesel oil distillate) Hydrofining Technology etc.
Wherein Hydrofining Technology mainly contains two kinds: a kind of is with the single hop hydrofining under middle pressure or low pressure of secondary processing diesel oil cut, the refining technique of diesel oil fraction hydrogenating is all disclosed such as FR2764902, RU2058371, US5068025, US5543036, US5817594, US5035793 etc., this technology can will make the sulphur content in the raw material drop to lower level, but the cetane value increase rate is very little, basically at 3～6 units, and the aromatic saturation degree is poor.Another kind is two sections purification techniquess that use noble metal catalyst, it can guarantee that sulphur, nitrogen in the diesel oil remove fully with aromatic hydrocarbons and removes in a large number in second segment in first paragraph, make sulphur in the product, nitrogen and aromaticity content reach requirement, such as US5556824 and US5651878 etc., but the one-time investment of its catalyzer and device is very huge, divide again two sections operations, operate very complicated, and the stability of catalyzer awaits further to verify, because volume space velocity is smaller, the processing power of device is limited in addition.
FCC raw material hydrogenation preconditioning technique can be avoided loss of octane number in the catalytic gasoline hydrogenation treating process, and has following advantage: the replacing speed that can reduce the FCC catalyzer; Reduce the FCC coke yield; Improving the FCC product distributes, improves the purpose product yield, reduces non-purpose product yield; Directly improve the FCC quality product, reduce the product sulphur content; Reduce the quantity discharged of FCC revivifier SOx, NOx etc., so FCC raw material hydrogenation pretreatment technology is widely used in modern refineries.Existing catalytically cracked material preconditioning technique mainly contains: US3983029 and US6793804 disclose hydroprocessing technique and catalyzer, CN1313379 discloses a kind of hydroprocessing process of poor-quality raw material for catalytic cracking, and CN1646665 discloses the hydrotreatment of hydrocarbon raw material.
Wax oil hydrogenation processing and two kinds of technological processs of hydrofining are independent operation in the prior art, although can satisfy the purpose requirement, because two cover processing unit (plant)s are fully independent, each own independently equipment and pipeline, certainly will cause total investment expenses high, the high deficiency of process cost.
Summary of the invention
For the deficiencies in the prior art, the invention provides a kind of comprehensive hydrodesulfurization method of hydrocarbon raw material, features for wax oil hydrogenation desulfurization and diesel oil hydrofining, both are combined, be implemented in and produce qualified diesel product and fine quality catalytic cracking raw material oil on the basis of reducing to greatest extent construction investment.
A kind of hydro-desulphurizing combined method, raw material comprise wax oil feedstock and diesel oil distillate oil raw material, comprise the steps:
A, under the hydrotreatment operational condition, wax oil stock oil is through the hydrotreating catalyst bed, the hydrotreatment reaction effluent separates in high pressure hot separator and obtains gas phase and liquid phase, gas phase comprises hydrogen and light hydrocarbons, liquid phase is the hydrogenation wax oil;
B, under the hydrofining operational condition, diesel raw material oil with after the gas phase that step a obtains is mixed through the Hydrobon catalyst bed;
C, step b reaction effluent enter gas-liquid separator, and gas phase recycles behind depriving hydrogen sulphide, and liquid phase enters the fractionating system fractionation and obtains various hydrocarbon productss.
It is 350～620 ℃ of heavy endss that the described wax oil stock oil of step a generally comprises boiling range, as being one or more in the various vacuum gas oils (VGO) that obtain in the petroleum refining process, deasphalted oil (DAO), coker gas oil (CGO), heavy cycle oil (HCO) etc., also can be from coal tar, gelatin liquefaction wet goods.
The described hydrotreating catalyst of step a is conventional hydrotreating catalyst, can be various commercial catalysts, as Fushun Petrochemical Research Institute (FRIPP) development and production 3926,3936, the hydrotreating catalyst such as CH-20,3996, FF-14, FF-16, FF-18, FF-26, the catalyzer such as HR-416, HR-448 of Compaynie Francaise des Petroles (IFP), the TK-525 of Denmark Tuo Pusuo company (Topsor), TK-557 catalyzer, KF-752, the KF-840 of He Lan Aksu company (AKZO), KF-901, KF-907 etc.The FH-FS of bulk phase catalyst such as Fushun Petrochemical Research Institute (FRIPP) development and production etc.Above-mentioned hydrotreating catalyst also can be prepared by this area knowledge, common hydrotreating catalyst (loaded catalyst, active metallic content is relatively low, generally count 20%～45% with oxide compound) general first Kaolinite Preparation of Catalyst carrier, then use pickling process supported active metal component, bulk phase catalyst (active metallic content is high, generally counts 50%～85% with oxide compound) generally adopts the coprecipitation method preparation.
The described hydrotreatment operational condition of step a is: reaction pressure 3.0～20.0MPa, hydrogen to oil volume ratio are 200: 1～2500: 1, and volume space velocity is 0.1～8.0h
-1, 260 ℃～455 ℃ of temperature of reaction; Preferred operational condition is reaction pressure 4.0～18.0MPa, hydrogen to oil volume ratio 300: 1～2000: 1, volume space velocity 0.2～6.0h
-1, 280～444 ℃ of temperature of reaction.The working pressure of high pressure hot separator is system pressure, and temperature is generally 180～410 ℃, is preferably 220～390 ℃.Contain the light hydrocarbons that the wax oil hydrogenation treating processes produces in the gas phase that high pressure hot separator is told, such as diesel oil distillate and gasoline fraction.
The described diesel oil of step b can comprise one or more mixing oil of straight-run diesel oil, coker gas oil, catalytic diesel oil, liquefied coal coil light ends etc., also can comprise the light ends such as straight-run spirit, coker gasoline, and its boiling range is generally 64 ℃～380 ℃.
The described hydrofining of step b can be adopted the common Hydrobon catalyst in this area, also can adopt high-activity hydrofining catalyst, also can adopt common Hydrobon catalyst and high-activity hydrofining catalyst to be used by suitable way.Catalyzer can be selected the commercial catalysts that suits, such as Hydrobon catalysts such as FH-5A, the FDS-4A of Fushun Petrochemical Research Institute's development and production, FH-98, FH-DS, FH-UDS, or by the existing method preparation in this area.
The described hydrofining operational condition of step b is generally: stagnation pressure 4.0MPa～18.0MPa, temperature of reaction is 260 ℃～440 ℃, volume space velocity 0.3h during liquid
-1～6.0h
-1, hydrogen to oil volume ratio is 100: 1～2000: 1.The pressure of step a is slightly high than the pressure of step b, and being convenient to hydrogen can tandem circulation, usually high 0.01～2.0MPa.
Compared with prior art, the present invention improves the quality of products different material oil by optimization technological process and operational condition under optimum, finally obtained desirable comprehensive process effect.In technical process, the inventive method and two kinds of raw materials add respectively man-hour relatively: the advantage such as have saving equipment (gas-liquid separation equipment, stripping apparatus, compressor etc.), technical process is short, facility investment is low, process cost is low.Wax oil hydrogenation is processed and is adopted hot high score flow process simultaneously, can save cold high score and the cold low equipment that grades, and two cover systems share hydrogen gas system and desulphurization system, can save make-up hydrogen compressor, circulating hydrogen compressor and a cover desulphurization system.The light hydrocarbons oil product that hydrotreatment obtains directly enters the hydrofining reaction district, further improves the quality of products, and can save the separation system equipment of this component.
Description of drawings
Fig. 1 is one embodiment of the present invention schematic flow sheets.
Embodiment
At first wax oil hydrogenation is processed stock oil 1 and is mixed into hydrotreating reactor 3 with hydrogen 2, obtains the low hydrotreatment resultants 4 of impurity such as sulfur-bearing, nitrogen.4 separate in high pressure hot separator 5 and obtain liquid hydrogenation wax oil and directly enter catalytic cracking unit, separate the gas phase (comprising hydrogen and light ends oil) 7 that obtains and are mixed into hydrofining reactor 9 with hydrofining diesel oil raw material 8.Through series reaction, obtain hydrofining resultant 10.Hydrofining resultant 10 separates the H 2 S-containing gas 12 that obtains and enters de-hydrogen sulfide column 13 in high-pressure separator 11, obtain circulation gas 14 behind the depriving hydrogen sulphide and use with new hydrogen 16 mixed cycle after through circulating hydrogen compressors 15 superchargings.Separate the liquid 17 that obtains in the high-pressure separator 11 and enter stripping tower 18 (if gasoline fraction is more in 8, can change separation column into), obtain gas products 19, gasoline (or petroleum naphtha) 20 and diesel product 21.
Below by specific embodiment, further specify the present invention program and effect.
Use the main character of stock oil to see Table 1, hydrotreatment operational condition and the results are shown in Table 2, hydrofining operational condition and structure see Table 3.
Table 1 stock oil character
| The stock oil title | Stock oil-1 | Stock oil-2 | Stock oil-3 | Stock oil-4 | ||
| The | Diesel oil | 1 | |
Coking gasoline and | Wax oil | 1 |
| Density (20 ℃)/gcm -3 | 0.8564 | 0.9302 | 0.8201 | 0.9352 | ||
| The boiling range scope, ℃ | 165～380 | 167～368 | 64～357 | 330～580 | ||
| Sulphur content, wt% | 1.46 | 0.78 | 0.95 | 2.45 | ||
| Nitrogen content, wt% | 0.05 | 0.12 | 0.07 | 0.15 | ||
| Cetane value | 45.5 | 25.1 | / | / | ||
| Aromaticity content, wt% | 35.3 | 70.4 | 15.9 | 59.1 |
Table 2 hydrotreatment operational condition and result
| Numbering | |
|
|
|
| Stock oil | Stock oil-4 | Stock oil-4 | Stock oil-4 | Stock oil-4 |
| Catalyzer | FF-14 | FF-14 | FF-18 | FF-18 |
| Reaction pressure/MPa | 8.0 | 6.0 | 15.0 | 12.0 |
| Average reaction temperature/℃ | 375 | 360 | 365 | 350 |
| LHSV/h -1 | 1.5 | 1.0 | 0.8 | 2.2 |
| Hydrogen to oil volume ratio (v/v) | 700∶1 | 1000∶1 | 1500∶1 | 500∶1 |
| The high pressure hot separator temperature, ℃ | 270 | 210 | 390 | 330 |
| The wax oil yield, wt% | 93.2 | 94.0 | 86.4 | 91.0 |
| Sulphur content/μ gg -1 | 2200 | 2900 | 240 | 750 |
Table 3 hydrofining operational condition and result
| Numbering | |
|
|
|
| Stock oil | Stock oil-1 | Stock oil-1 | Stock oil-2 | Stock oil-3 |
| Catalyzer | FH-98 | FH-98 | FH-98 | FH-UDS |
| Reaction pressure/MPa | 7.5 | 5.7 | 14.3 | 11.5 |
| Temperature of reaction/℃ | 350 | 340 | 370 | 345 |
| LHSV/h -1 | 2.0 | 1.5 | 1.5 | 3.5 |
| Hydrogen to oil volume ratio (v/v) | 300∶1 | 600∶1 | 800∶1 | 400∶1 |
| ＜145 ℃ of naphtha fractions | ||||
| Sulphur content/μ gg -1 | 65 | 50 | ＜10 | ＜1 |
| 〉=145 ℃ of diesel oil distillates | ||||
| Density (20 ℃)/gcm -3 | 0.8345 | 0.8352 | 0.8665 | 0.8204 |
| Sulphur content/μ gg -1 | 110 | 80 | 15 | 8 |
| Cetane value | 51.5 | 51.0 | 45.1 | 54.6 |
From above embodiment, can find out, the maximum characteristics of this combination process are, rationally utilize the features of hydroprocessing technique and hydrofining technology, when keeping the different device desulfurization to require, owing to adopted combination process, greatly reduced facility investment and the process cost of device.Simultaneously, the light hydrocarbons that the wax oil hydrogenation treating processes is produced directly enters Diesel Oil Hydrofining Unit behind hot high score, can improve the diesel product quality on the one hand, saved on the other hand separating device, and greatly improved the utilization ratio of heat owing to do not need the air-cooler cooling, reduced plant energy consumption.
Claims (8)
1. hydro-desulphurizing combined method, raw material comprise wax oil feedstock and diesel oil distillate oil raw material, comprise the steps:
A, under the hydrotreatment operational condition, wax oil stock oil is through the hydrotreating catalyst bed, the hydrotreatment reaction effluent separates in high pressure hot separator and obtains gas phase and liquid phase, gas phase comprises hydrogen and light hydrocarbons, liquid phase is the hydrogenation wax oil; The high pressure hot separator temperature is 180～410 ℃;
B, under the hydrofining operational condition, diesel raw material oil with after the gas phase that step a obtains is mixed through the Hydrobon catalyst bed;
C, step b reaction effluent enter gas-liquid separator, and gas phase recycles behind depriving hydrogen sulphide, and liquid phase enters the fractionating system fractionation and obtains various hydrocarbon productss;
Wherein the described diesel raw material oil of step b comprises one or more in straight-run diesel oil, coker gas oil, catalytic diesel oil, the liquefied coal coil light ends, also contains straight-run spirit or coker gasoline in the diesel raw material oil.
2. in accordance with the method for claim 1, it is characterized in that the described wax oil stock oil of step a is one or more in vacuum gas oil, deasphalted oil, coker gas oil, the heavy cycle oil, perhaps from coal tar or liquefied coal coil.
3. in accordance with the method for claim 1, it is characterized in that the described hydrotreatment operational condition of step a is: reaction pressure 3.0～20.0MPa, hydrogen to oil volume ratio are 200: 1～2500: 1, and volume space velocity is 0.1～8.0h
-1, 260 ℃～455 ℃ of temperature of reaction.
4. in accordance with the method for claim 1, it is characterized in that the described hydrotreatment operational condition of step a is: reaction pressure 4.0～18.0MPa, hydrogen to oil volume ratio 300: 1～2000: 1, volume space velocity 0.2～6.0h
-1, 280～444 ℃ of temperature of reaction, high pressure hot separator temperature are 220～390 ℃.
5. in accordance with the method for claim 1, it is characterized in that containing in high pressure hot separator is told among the step a the gas phase diesel oil distillate and the gasoline fraction that the wax oil hydrogenation treating processes produces.
6. in accordance with the method for claim 1, it is characterized in that the described hydrofining operational condition of step b is: stagnation pressure 4.0MPa～18.0MPa, temperature of reaction is 260 ℃～440 ℃, volume space velocity 0.3h during liquid
-1～6.0h
-1, hydrogen to oil volume ratio is 100: 1～2000: 1.
7. according to claim 1,3 or 6 described methods, it is characterized in that the pressure of step a than the high 0.01～2.0MPa of pressure of step b, being convenient to hydrogen can the tandem circulation.
8. in accordance with the method for claim 1, it is characterized in that step c is described through using with new hydrogen mixed cycle after the supercharging of gas phase process circulating hydrogen compressor behind the depriving hydrogen sulphide.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN101942327B (en) * | 2009-07-09 | 2013-05-01 | 中国石油化工股份有限公司 | Hydrotreatment combination technology for producing ultra low sulfur diesel |
| CN102465030B (en) * | 2010-11-05 | 2014-07-23 | 中国石油化工股份有限公司 | Hydrogenation process combination method |
| CN102876366B (en) * | 2011-07-11 | 2015-08-12 | 中国石油化工股份有限公司 | A kind of Unionfining treatment process |
| CN103074103A (en) * | 2011-10-26 | 2013-05-01 | 中国石油化工股份有限公司 | A combined hydroprocessing method |
| CN103773453B (en) * | 2012-10-24 | 2016-03-30 | 中国石油化工股份有限公司 | A kind of inferior raw material hydroprocessing process |
| CN109988602A (en) * | 2017-12-29 | 2019-07-09 | 中国石油化工股份有限公司 | A kind of flexible wax oil hydrogenation treatment process |
| CN109988634B (en) * | 2017-12-29 | 2021-05-04 | 中国石油化工股份有限公司 | Residual oil hydrotreating and hydrofining combined process |
| CN109988615B (en) * | 2017-12-29 | 2021-07-09 | 中国石油化工股份有限公司 | Flexible wax oil hydrotreating process |
| CN109988624B (en) * | 2017-12-29 | 2021-07-09 | 中国石油化工股份有限公司 | Residual oil hydrotreating and hydrofining combined process |
| CN109988646B (en) * | 2017-12-29 | 2022-07-12 | 中国石油化工股份有限公司 | Wax oil hydrotreating and hydrofining combined process |
| CN109988614B (en) * | 2017-12-29 | 2021-07-09 | 中国石油化工股份有限公司 | Flexible residual oil hydrotreating process |
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| CN1260376A (en) * | 1999-03-08 | 2000-07-19 | 中国石化集团洛阳石油化工工程公司 | Converting and combining method for hydrogenation of hydrocarbon |
| CN1458233A (en) * | 2002-05-15 | 2003-11-26 | 中国石油化工股份有限公司 | Process for coking full fraction oil hydrogenation refining |
| US7108779B1 (en) * | 2003-09-25 | 2006-09-19 | Uop Llc | Hydrocarbon desulfurization process |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1260376A (en) * | 1999-03-08 | 2000-07-19 | 中国石化集团洛阳石油化工工程公司 | Converting and combining method for hydrogenation of hydrocarbon |
| CN1458233A (en) * | 2002-05-15 | 2003-11-26 | 中国石油化工股份有限公司 | Process for coking full fraction oil hydrogenation refining |
| US7108779B1 (en) * | 2003-09-25 | 2006-09-19 | Uop Llc | Hydrocarbon desulfurization process |
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