CN103789029B - Two-phase hydrogenation combination method - Google Patents
Two-phase hydrogenation combination method Download PDFInfo
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- CN103789029B CN103789029B CN201210432653.8A CN201210432653A CN103789029B CN 103789029 B CN103789029 B CN 103789029B CN 201210432653 A CN201210432653 A CN 201210432653A CN 103789029 B CN103789029 B CN 103789029B
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Abstract
The invention provides a two-phase hydrogenation combination method. The method combines a traditional gas-phase circulating hydrogenation technology and a two-phase hydrogenation technology and processes different raw materials according to advantages of each of the technologies. The middle part of a high-pressure separator of a traditional gas-phase circulating hydrogenation unit is provided with a partition plate to divide the high-pressure separator into a gas-liquid separating chamber and a hydrogen dissolution chamber. Middle distillate oil which is difficult to remove impurities is processed by adoption of the gas-phase circulating hydrogenation technology. Produced materials are fed into the gas-liquid separation chamber to perform gas-liquid separation. The separated liquid phase is fed into a distillation system. The separated gas phase is lead to the bottom of the hydrogen dissolution chamber through a pipeline, and is subjected to countercurrent contact with raw materials of the two-phase hydrogenation unit and circulating oil which are fed from the upper part of the hydrogen dissolution chamber. The hydrogen-dissolved raw materials of the two-phase hydrogenation unit and the hydrogen-dissolved circulating oil are fed into a two-phase hydrogenation reactor to perform hydrogenation. Compared with the prior art, the method can effectively solve a problem of hydrogenation inhibition caused by accumulated hydrogen sulfide in the two-phase hydrogenation unit.
Description
Technical field
The present invention relates to a kind of two-phase hydrogenation combined method, the particularly combined hydrogenation method of different mass distillate feedstock.
Background technology
Along with the continuous enhancing of people's environmental consciousness, environmental law Laws & Regulations requires more strict to engine exhaust emission, various standard of fuel requires that the content of S, N is also harsher.Simultaneously due to the continuous increase of Oil extraction amount and the continuous minimizing of conventional crude reserves, crude oil in poor quality trend is more and more serious, how the S of the intermediate oil that crude oil straight run distillation obtains and the middle runnings that the secondary processing such as coking, catalytic cracking obtains, N content also corresponding increase, be processed into the major issue that the product Shi Ge refinery that meets environmental requirement faces by middle runnings higher for the foreign matter content such as sulphur, nitrogen.
Hydrogenation process is the most economical effective scheme removing middle runnings impurity.Existing most of hydrogenation unit all adopts higher hydrogen-oil ratio and hydrogen dividing potential drop, to ensure the catalyst runs life-span, promotes the reactions such as hydrogenating desulfurization, denitrogenation, aromatic saturation and cracking.But the higher hydrogen gas circulating system of pressure needs high investment cost and running cost, indirectly adds oil manufacture cost.This traditional hydrogen addition technology is gas (being mainly hydrogen), liquid (stock oil), solid (catalyzer) phase reaction in reaction process, reactor types generally comprises trickle bed, ebullated bed, expanded bed, adverse current bed etc., its principal feature is amounts of hydrogen considerably beyond reaction institute expense, and a large amount of unreacting hydrogen recycles.Be referred to as gas phase circulation hydrogen addition technology in this patent, corresponding device is called gas phase circulation hydrogenation unit.
Along with technician is to the understanding that deepens continuously of hydrogen addition technology, a kind of two-phase hydrogenation technology is developed.In raw material and thinning oil, dissolve supersaturation hydrogen, directly enter reactor and carry out hydrogenation reaction, cancel recycle hydrogen system, reduce costs.Owing to eliminating recycle hydrogen system, so the adaptability of this technique to raw material has certain limitation.This technology is mainly two-phase in reaction process, i.e. liquid phase (stock oil and thinning oil) and solid phase (catalyzer), and claim this technique to be two-phase hydrogenation technology in this patent, corresponding device is called two-phase hydrogenation device.
US6881326 describes a kind of two-phase hydrogenation preconditioning technique.Its technological process is that hydrogen is dissolved in oil through a mixed hydrogen production device by fresh feed oil, turning oil and hydrogen, and the oil of dissolving hydrogen enters less reactor and catalyst exposure carries out hydrogenation reaction, deviates from the impurity in oil.After reaction, a logistics part is circulated to mixed hydrogen production device, and a part is discharged from device as product.Required hydrogen is dissolved in oil before adopting raw material and turning oil to enter reactor by this method in advance, can omit recycle hydrogen system.During the method process secondary processing intermediate oil, impurity extrusion rate is difficult to up to standard.In existing two-phase hydrogenation technology, the hydrogen sulfide be dissolved in oil phase is difficult to effective elimination, and in reactive system, circulation accumulation, causes more serious restraining effect to hydrogenation reaction.Although can adopt as the methods such as stripping remove, owing to being in High Temperature High Pressure system, facility investment and process cost can be increased equally.
Summary of the invention
For the deficiencies in the prior art, the invention provides a kind of two-phase hydrogenation combined method.Hydrogenation technique and the two-phase hydrogenation technique of conventional gas-phase being circulated combines, according to respective advantage, and processing different material.
A kind of two-phase hydrogenation combined method of the present invention, gas phase circulation hydrogenation unit is combined with two-phase hydrogenation device, specifically comprises following content:
A) high-pressure separator of gas phase circulation hydrogenation unit is middle arranges vertical partition plate, high-pressure separator is divided into gas-liquid separation chamber and molten hydrogen room two portions;
B) distillate feedstock is divided into high sulfur content distillate feedstock and low sulfur content distillate feedstock by sulphur content, high sulfur content distillate feedstock adopts gas phase circulation hydrogen addition technology to process, material after the process of gas phase circulation hydrogen addition technology enters gas-liquid separation chamber and carries out gas-liquid separation, and isolated liquid phase enters product recovery; Gas phase introduces the bottom of molten hydrogen room by pipeline, contacts with two-phase hydrogenation device turning oil with the low sulfur content distillate feedstock entering molten hydrogen room, and the gas phase that top, molten hydrogen room is discharged enters the recycle hydrogen system of gas phase circulation hydrogenation unit;
C) the low sulfur content distillate feedstock after molten hydrogen and turning oil escape and enter two-phase hydrogenation reactor and carry out hydrogenation reaction bottom molten hydrogen room, reclaim hydrogenation after cut oil production from two-phase hydrogenation reactor reaction effluent.
Step a) described in dividing plate gas phase is circulated hydrogenation unit high-pressure separator be divided into two independently containers, gas-liquid separation chamber top is connected with bottom molten hydrogen room by pipeline.The indoor gas phase of molten hydrogen flows from bottom to top, and with liquid phase counter current contact, molten hydrogen indoor can arrange filler or cross-flow inner member, to increase molten hydrogen effect and to remove the hydrogen sulfide in turning oil.The working pressure identical with gas phase circulation hydrogenation unit reaction pressure (ignoring the Pressure Drop that Flow of Goods and Materials produces) of high-pressure separator.The service temperature of high-pressure separator can be 40 DEG C to gas phase circulation hydrogenation unit temperature of reaction.
Step b) described in high sulfur content distillate feedstock and low sulfur content distillate feedstock sulphur content by 1000 ~ 12000 μ g/g preferably in 2000 ~ 8500 μ g/g arbitrary value divide, higher than divide value is high sulfur content distillate feedstock, and lower than divide value is low sulfur content distillate feedstock.High sulfur content distillate feedstock comes from secondary processing distillate usually, as one or more in coking distillate, catalytic cracking distillate, coal liquefaction fraction wet goods; Low sulfur content distillate feedstock is generally the straight run wet goods that crude distillation obtains, and also can mix a small amount of secondary processing distillate.The boiling range scope of high sulfur content distillate feedstock and low sulfur content distillate feedstock is generally one or more in kerosene(oil)fraction, diesel oil distillate, reduced pressure distillate oil distillate etc., within the scope of being preferably 130 ~ 450 DEG C, most preferably is within the scope of 200 ~ 380 DEG C.
Step b) described gas phase circulation hydrogen addition technology operational condition is: temperature of reaction 100 ~ 400 DEG C, preferably 260 ~ 380 DEG C; Reaction pressure 2.5 ~ 10.0MPa, preferably 4.0 ~ 8.0MPa; Preferred gas phase circulation hydrogen addition technology reaction pressure is higher than the reaction pressure 1 ~ 4MPa of two-phase hydrogenation device; Hydrogen to oil volume ratio 50:1 ~ 1000:1, preferred 300:1 ~ 800:1; Volume space velocity 0.6 ~ 5.0h
-1, preferably 1.0 ~ 2.5h
-1.Gas phase circulation hydrogen addition technology can adopt suitable reactor types, as trickle-bed reactor, and ebullated bed reactor, expanded bed reactor, adverse current bed bioreactor etc.
Step c) charging of described two-phase hydrogenation device reaction device can adopt the operating method of upper feeding bottom discharge, also can adopt the operating method of lower charging top discharge.Step c) described two-phase hydrogenation device operational condition is: temperature of reaction 100 ~ 400 DEG C, preferably 260 ~ 380 DEG C; Reaction pressure 1.5 ~ 8.0MPa, preferably 2.0 ~ 6.0MPa; Volume space velocity 0.6 ~ 5.0h
-1, preferably 1.0 ~ 2.5h
-1; Turning oil and fresh feed volumetric mixture ratio are 0.5:1 ~ 6.0:1, preferred 1.0:1 ~ 3.0:1.
The catalyzer that above-mentioned steps uses is the hydrotreating catalyst of this area routine, wherein the active metal component of catalyzer can be nickel, cobalt, molybdenum or tungsten etc. one or more, catalyzer carries out sulfidizing before use, and active metal component is converted into sulphided state.Catalyzer composition can comprise by weight percentage: nickel or cobalt are that 0.5% ~ 10%(calculates by its oxide compound), molybdenum or tungsten are that 1% ~ 25%(calculates by its oxide compound), carrier can be aluminum oxide, silicon oxide, aluminium oxide-silicon oxide, titanium oxide etc. one or more.Catalyzer is extrudate or spherical.The bulk density of catalyzer is 0.5 ~ 1.1g/cm
3, catalyst particle diameter (spherical diameter or bar shaped diameter) is 0.04 ~ 1.0mm, and specific surface area is 80 ~ 350m
2/ g.Gas phase circulation hydrotreatment and two-phase hydrogenation process occur reaction is mainly hydrogenating desulfurization, hydrodenitrification, Alkene hydrogenation is saturated, aromatic hydrogenation is saturated.
The high-pressure separator of conventional gas-phase circulation hydrogen addition technology of the present invention both completed gas-liquid separation, achieved again the molten hydrogen function of two-phase hydrogenation raw material and turning oil.Although be separated the certain hydrogen sulfide of gas phase containing the generation of gas phase circulation hydrogenation process obtained in high-pressure separator in gas-liquid separation chamber, but when contacting with two-phase hydrogenation device turning oil, still can the most hydrogen sulfide in turning oil be transferred in gas phase, hydrogen sulfide content in turning oil is reduced greatly, avoids sulfuration sulphur in two-phase hydrogenation reaction process and accumulate the problem of the inhibited reaction caused.Hydrogen make-up needed for reaction process can add in gas phase circulation hydrogenation system.
The advantage of a kind of two-phase hydrogenation combined method of the present invention is:
1, hydrogen addition technology and the two-phase hydrogenation technique of conventional gas-phase being circulated combines, according to respective advantage, and processing different material.Two-phase hydrogenation dress eliminates molten hydrogen system, reduces investment outlay and process cost.
2, relative to two-phase hydrogenation device, the liquid phase in the molten hydrogen room of conventional gas-phase circulation hydrogenation unit high-pressure separator is hydrogen hypersaturated state, can provide more reaction hydrogen for two-phase hydrogen device, improves the impurity removal percentage of raw material.
3, in conventional gas-phase circulation hydrogenation unit high-pressure separator, owing to there is a large amount of hydrogen, the most of hydrogen sulfide in two-phase hydrogenation charging can be carried discharge, less to the catalysts influence of two-phase hydrogenation reactor.And employing has in the two-phase hydrogenation technology of liquid phase circulation system, the hydrogen sulfide in turning oil is difficult to effective elimination, on deep hydrodesulfurizationof impact obviously.
Accompanying drawing explanation
Fig. 1 is the schematic flow sheet of a kind of two-phase hydrogenation combined method of the present invention.
Sequence number 1 is gas phase circulation hydrogenation unit reactor, 2 is gas phase circulation hydrogenation unit high-pressure separator, 3 is gas phase circulation hydrogenation unit high-pressure separator dividing plate, 4 is two-phase hydrogenation device reaction device, 5 isolate liquid phase for gas phase circulation hydrogenation unit high-pressure separator, and 6 is high sulfur content distillate feedstock, and 7 is low sulfur content distillate feedstock, 8 is two-phase hydrogenation device reaction generation oil, and 9 is two-phase hydrogenation device turning oil.
Embodiment
In the middle of the high-pressure separator of conventional gas-phase circulation hydrogenation unit, dividing plate is set, high-pressure separator is divided into gas-liquid separation chamber and molten hydrogen room two portions.The distillate feedstock of high sulfur content adopts traditional mesohigh gas phase circulation hydrogenation technique processing, generation material enters gas-liquid separation chamber and carries out gas-liquid separation, isolated liquid phase enters product recovery, the bottom that gas phase introduces molten hydrogen room by pipeline (can arrange internal pipeline also, can external pipe be set), the low sulfur content distillate feedstock entered with middle and upper part, molten hydrogen room and turning oil carry out counter current contact, are then entered the recycle hydrogen system of gas phase circulation hydrogenation unit by top, molten hydrogen room.Low sulfur content distillate feedstock after molten hydrogen and turning oil enter two-phase hydrogenation reactor and carry out hydrogenation reaction.
For setting forth specific features of the present invention further, will be illustrated by reference to the accompanying drawings.
By reference to the accompanying drawings 1, a kind of two-phase hydrogenation combined method of the present invention process is:
Conventional gas-phase circulation hydrogenation unit high-pressure separator 2 is divided into gas-liquid separation chamber and molten hydrogen room by dividing plate 3.After high sulfur content distillate feedstock 6 and recycle hydrogen mix, enter conventional gas-phase circulation hydrogenation unit reactor 1, after hydrogenation, logistics enters the gas-liquid separation chamber of high-pressure separator 2, isolated liquid phase 5 enters fractionating system, gas phase enters bottom the molten hydrogen room of dividing plate 3 opposite side by pipeline, contact with turning oil 9 is reverse with low sulfur content distillate feedstock 7 from bottom to top, then gas phase enters conventional gas-phase circulation hydrogenation unit recycle hydrogen system.The two-phase hydrogenation raw material 7 of dissolving hydrogen and turning oil 9 enter two-phase hydrogenation reactor 4 and carry out hydrogenation reaction, reclaim hydrogenation after cut oil production from two-phase hydrogenation reactor reaction effluent 8.
For further illustrating the solution of the present invention and effect, enumerate following examples:
Embodiment
The present embodiment is a kind of embodiment of two-phase hydrogenation combined method, and operating process schematic diagram is with reference to accompanying drawing 1.
Test uses feedstock property in table 1.Tradition hydrogenator and two-phase hydrogenation reactor adopt identical catalyzer, and catalyst property is in table 2.Tradition hydrogenation unit, two-phase hydrogenation device reaction condition and generation oil nature are in table 3.
Comparative example
The same embodiment of raw material of two-phase hydrogenation device, adopts turning oil and raw material to mix the operating method of molten hydrogen.
Table 1 stock oil character
| Oil property | High sulfur content distillate feedstock (gas phase circulation hydrogenation unit raw material) | Low sulfur content distillate feedstock (two-phase hydrogenation device raw material) |
| Density (20 DEG C)/gcm -3 | 0.8554 | 0.8378 |
| Boiling range scope/DEG C | 170～372 | 159～346 |
| Sulphur/μ gg -1 | 9746 | 5728 |
| Nitrogen/μ gg -1 | 366 | 129 |
Table 2 catalyzer physico-chemical property
| Project | Data |
| Catalyst activity component | Mo、Ni、W |
| Active component content (in oxide weight), % | 29 |
| Carrier | Aluminum oxide |
| Shape | Trifolium |
| Diameter | 3.1 |
| Pore volume/mLg -1 | 0.41 |
| Specific surface area/m 2·g -1 | 235 |
Table 3 hydrofining technology condition
| Processing condition | Gas phase circulation hydrogenation unit | Two-phase hydrogenation device | Comparative example |
| Reaction pressure/MPa | 6.5 | 6.0 | 6.0 |
| Temperature of reaction/DEG C | 360 | 345 | 345 |
| Two-phase hydrogenation charge ratio | 2:1* | 2:1* | |
| Hydrogen to oil volume ratio | 550:1 | ||
| Volume space velocity/h -1(relative fresh feed) | 1.5 | 1.5 | 1.5 |
| Generate oil nature: | |||
| S，μg/g | 8.6 | 12.9 | 327.5 |
| N，μg/g | 2.9 | 5.2 | 40.7 |
| Boiling range scope, DEG C | 167～363 | 150～340 | 150～342 |
* two-phase hydrogenation reactor discharges the volume ratio of liquid phase internal circulating load and the fresh feed of two-phase hydrogenation device.
Claims (14)
1. a two-phase hydrogenation combined method, gas phase circulation hydrogenation unit is combined with two-phase hydrogenation device, it is characterized in that comprising following content:
A) high-pressure separator of gas phase circulation hydrogenation unit is middle arranges vertical partition plate, high-pressure separator is divided into gas-liquid separation chamber and molten hydrogen room two portions;
B) distillate feedstock is divided into high sulfur content distillate feedstock and low sulfur content distillate feedstock by sulphur content, high sulfur content distillate feedstock adopts gas phase circulation hydrogen addition technology to process, material after the process of gas phase circulation hydrogen addition technology enters gas-liquid separation chamber and carries out gas-liquid separation, and isolated liquid phase enters product recovery; Gas phase introduces the bottom of molten hydrogen room by pipeline, contacts with two-phase hydrogenation device turning oil with the low sulfur content distillate feedstock entering molten hydrogen room, and the gas phase that top, molten hydrogen room is discharged enters the recycle hydrogen system of gas phase circulation hydrogenation unit; Described high sulfur content distillate feedstock and the sulphur content of low sulfur content distillate feedstock divide by arbitrary value in 1000 ~ 12000 μ g/g;
C) the low sulfur content distillate feedstock after molten hydrogen and turning oil escape and enter two-phase hydrogenation reactor and carry out hydrogenation reaction bottom molten hydrogen room, reclaim hydrogenation after cut oil production from two-phase hydrogenation reactor reaction effluent.
2. method according to claim 1, is characterized in that: step a) described in dividing plate gas phase is circulated hydrogenation unit high-pressure separator be divided into two independently containers, gas-liquid separation chamber top is connected with bottom molten hydrogen room by pipeline.
3. method according to claim 1 and 2, is characterized in that: the indoor gas phase of molten hydrogen flows from bottom to top, and with liquid phase counter current contact, molten hydrogen indoor arrange filler or cross-flow inner member, to increase molten hydrogen effect and to remove the hydrogen sulfide in turning oil.
4. method according to claim 1, it is characterized in that: step b) described in high sulfur content distillate feedstock and low sulfur content distillate feedstock sulphur content by 2000 ~ 8500 μ g/g arbitrary value divide, higher than divide value is high sulfur content distillate feedstock, and lower than divide value is low sulfur content distillate feedstock.
5. the method according to claim 1 or 4, is characterized in that: the boiling range scope of high sulfur content distillate feedstock and low sulfur content distillate feedstock is one or more in kerosene(oil)fraction, diesel oil distillate, reduced pressure distillate oil distillate.
6. method according to claim 5, is characterized in that: the boiling range scope of high sulfur content distillate feedstock and low sulfur content distillate feedstock is 130 ~ 450 DEG C.
7. method according to claim 5, is characterized in that: the boiling range scope of high sulfur content distillate feedstock and low sulfur content distillate feedstock is 200 ~ 380 DEG C.
8. method according to claim 1, is characterized in that: step b) gas phase circulation hydrogen addition technology operational condition is: temperature of reaction 100 ~ 400 DEG C; Reaction pressure 2.5 ~ 10.0MPa; Hydrogen to oil volume ratio 50:1 ~ 1000:1; Volume space velocity 0.6 ~ 5.0h
-1.
9. method according to claim 1, is characterized in that: step b) gas phase circulation hydrogen addition technology operational condition is: temperature of reaction 260 ~ 380 DEG C; Reaction pressure 4.0 ~ 8.0MPa; Hydrogen to oil volume ratio 300:1 ~ 800:1; Volume space velocity 1.0 ~ 2.5h
-1.
10. method according to claim 1, is characterized in that: the reactor types that gas phase circulation hydrogenation adopts is trickle-bed reactor, ebullated bed reactor, expanded bed reactor or adverse current bed bioreactor.
11. methods according to claim 1, is characterized in that: step c) charging of two-phase hydrogenation device reaction device adopts the operating method of upper feeding bottom discharge, or adopts the operating method of lower charging top discharge.
12. methods according to claim 1, is characterized in that: step c) described two-phase hydrogenation device operational condition is: temperature of reaction 100 ~ 400 DEG C; Reaction pressure 1.5 ~ 8.0MPa; Volume space velocity 0.6 ~ 5.0h
-1; Turning oil and fresh feed volumetric mixture ratio are 0.5:1 ~ 6.0:1.
13. methods according to claim 1, is characterized in that: step c) described two-phase hydrogenation device operational condition is: temperature of reaction 260 ~ 380 DEG C; Reaction pressure 2.0 ~ 6.0MPa; Volume space velocity 1.0 ~ 2.5h
-1; Turning oil and fresh feed volumetric mixture ratio are 1.0:1 ~ 3.0:1.
14. methods according to claim 1, it is characterized in that: the hydrotreating catalyst that the catalyzer that gas phase circulation hydrogenation unit and two-phase hydrogenation device use is this area routine, wherein the active metal component of catalyzer is one or more in nickel, cobalt, molybdenum or tungsten, catalyzer carries out sulfidizing before use, and active metal component is converted into sulphided state; Catalyzer composition comprises by weight percentage: nickel or cobalt count 0.5% ~ 10% with oxide weight, and molybdenum or tungsten count 1% ~ 25% with oxide weight; Carrier is aluminum oxide, silicon oxide, one or more in aluminium oxide-silicon oxide and titanium oxide.
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Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101280218A (en) * | 2008-06-02 | 2008-10-08 | 中国石油化工集团公司 | Two-phase hydrogenation method for hydrocarbon oil |
| CN102115678A (en) * | 2010-01-06 | 2011-07-06 | 中国石油化工集团公司 | Hydrogenation and desulfurization method of diesel oil and device thereof |
| CN102311790A (en) * | 2010-07-07 | 2012-01-11 | 中国石油化工股份有限公司 | Liquid phase circular hydrogenation treatment method capable of improving mixed amount of hydrogen |
| CN102311791A (en) * | 2010-07-07 | 2012-01-11 | 中国石油化工股份有限公司 | Liquid-phase circulating hydrogenation treatment method capable of reinforcing gas-liquid mass transfer |
| CN102465012A (en) * | 2010-11-05 | 2012-05-23 | 中国石油化工股份有限公司 | Inferior diesel oil deep hydrodesulfurization method |
| CN102465011A (en) * | 2010-11-05 | 2012-05-23 | 中国石油化工股份有限公司 | Hydrotreatment method of heavy distillate oil |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
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| US20080159928A1 (en) * | 2006-12-29 | 2008-07-03 | Peter Kokayeff | Hydrocarbon Conversion Process |
| US7927480B2 (en) * | 2008-01-29 | 2011-04-19 | Catalytic Distillation Technologies | Process for desulfurization of cracked naphtha |
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Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101280218A (en) * | 2008-06-02 | 2008-10-08 | 中国石油化工集团公司 | Two-phase hydrogenation method for hydrocarbon oil |
| CN102115678A (en) * | 2010-01-06 | 2011-07-06 | 中国石油化工集团公司 | Hydrogenation and desulfurization method of diesel oil and device thereof |
| CN102311790A (en) * | 2010-07-07 | 2012-01-11 | 中国石油化工股份有限公司 | Liquid phase circular hydrogenation treatment method capable of improving mixed amount of hydrogen |
| CN102311791A (en) * | 2010-07-07 | 2012-01-11 | 中国石油化工股份有限公司 | Liquid-phase circulating hydrogenation treatment method capable of reinforcing gas-liquid mass transfer |
| CN102465012A (en) * | 2010-11-05 | 2012-05-23 | 中国石油化工股份有限公司 | Inferior diesel oil deep hydrodesulfurization method |
| CN102465011A (en) * | 2010-11-05 | 2012-05-23 | 中国石油化工股份有限公司 | Hydrotreatment method of heavy distillate oil |
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