CN109777502A - Refinery gas adds hydrogen combinational processing method - Google Patents
Refinery gas adds hydrogen combinational processing method Download PDFInfo
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- CN109777502A CN109777502A CN201711118817.9A CN201711118817A CN109777502A CN 109777502 A CN109777502 A CN 109777502A CN 201711118817 A CN201711118817 A CN 201711118817A CN 109777502 A CN109777502 A CN 109777502A
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Abstract
The present invention discloses a kind of refinery gas and adds hydrogen combinational processing method, including following content :(a) diesel raw material oil is mixed in molten hydrogen storage equipment with hydrogen with recycle oil, subsequently into hydrogenator Hydrobon catalyst and catalyst for hydro-upgrading bed reacted under liquid-phase hydrogenatin operating condition；(b) reaction stream that step (a) obtains is reacted under liquid-phase hydrogenatin operating condition with after refinery gas and hydrogen mixing into the hydrogenation catalyst bed in supplement hydrogenator in molten gas equipment；(c) step (b) hydrogenation reaction effluent is separated into gas phase and liquid phase, continue the refinery gas after isolated hydrogen, hydrotreating after isolated gas phase removal hydrogen sulfide, isolated liquid phase is fractionated to obtain naphtha and cleaning diesel oil, and the isolated liquid phase of the hydrogenation reaction logistics and/or partial high pressure separator that the hydrogenation reaction effluent and/or part steps (b) that part steps (a) obtain obtain returns in molten hydrogen storage equipment as recycle oil.This method hydrotreating refinery gas and production can clean diesel oil simultaneously.
Description
Technical field
The invention belongs to the hydrogenation technique of oil Refining Technologies, it is related to a kind of refinery gas and adds hydrogen combinational processing method, specifically
It says and is related to the combined hydrogenation method of a kind of refinery gas's hydrotreating and production cleaning diesel oil.
Background technique
The energy in global range is mainly derived from fossil energy at present, and wherein petroleum is the main next of automotive fuel
Source.Need to produce a large amount of lightweights cleaning automotive fuels as world economy sustainable development, environmental regulation are increasingly strict, these will
It asks and existing oil Refining Technologies is improved.Diesel quality requirement as important automotive fuel is even more higher and higher,
Especially there is stringent limitation to the content of sulfur content, density, condensed-nuclei aromatics etc., hydro-upgrading of inferior diesel technology can be substantially
Degree reduces the sulfur content and arene content of diesel product, and reduces density, reduces condensation point and improve Cetane number.
Diesel oil hydrogenation modification technology is to improve the most important means of poor-quality diesel-oil by cut fraction quality and production cleaning diesel oil, liquid phase
Diesel oil hydrogenation technology can reach the requirement of cleaning diesel production in the case where energy consumption is greatly lowered.US6213835 and
US6428686 discloses a kind of hydrogenation technique of molten hydrogen in advance, and CN104560132A discloses a kind of Continuous Liquid Phase diesel oil hydrogenation
Processing method, CN104927902A disclose a kind of diesel oil hydrotreating method, and this method is more focused on hydrogen and is dissolved in diesel oil
In raw material, these methods be all be to be dissolved in hydrogen in diesel raw material carrying out hydrogenation reaction, there is no to reacting remaining hydrogen
Gas is utilized, directly in addition processing after separation.
Refinery gas generally comprises dry gas and liquefied gas etc., and there are many paths for its utilization.Wherein main purposes includes dry
Gas adds the raw material after hydrogen as preparing ethylene by steam cracking, and liquefied gas adds suitable as the raw material of preparing ethylene by steam cracking, synthesis after hydrogen
Raw material, motor liquified gas of acid anhydride etc..In existing REFINERY GAS technology, it is dry that CN201410271572.3 discloses a kind of coking
Gas hydrogenation catalyst and grading method of catalyst.This method is to solve the controlling party of reaction temperature when coking dry gas adds hydrogen
Method, but reaction process temperature rise is larger.CN201010221244.4 discloses a kind of hydrogenation of liquefied petroleum gas and prepares cracking of ethylene
The method of material is arranged two reactors, cooling facility is arranged between reactor, and CN201310628425.2 discloses a kind of liquefaction
The high-temperature hydrogenation purification process of gas material, by adding the method for hydrogen to carry out alkene saturation and hydrogenation and removing impurity.It is well known that alkene
The hydrogenation reaction of the unsaturated hydrocarbons such as hydrocarbon, alkadienes, alkynes is strong exothermal reaction, and temperature rise is all very big in gas hydrogenation process, is led to
Normal 100 ~ 200 DEG C, the balance of hydrogenation reaction is destroyed as the temperature rises, and seriously increases the generation of carbon distribution, thus
Reduce the service life of catalyst.
CN201010221263.7 discloses a kind of liquefied petroleum gas-coke gasoline hydrogenation combined process method, this method
It for combined method, but is not the method using liquid-phase hydrogenatin, coker gasoline mixes that carry out fixed bed hydrogenation anti-with hydrogen first
It answers, is hydrogenated to object and liquefied gas is mixed into other reactor, only address only the problem of liquefied gas adds hydrogen temperature rise.
In conclusion REFINERY GAS treatment process is gas phase reaction in the prior art, diesel oil hydrogenation is liquid phase reactor,
The two reaction type is entirely different, and therefore, REFINERY GAS processing and diesel oil liquid-phase hydrogenatin modification combined method are rarely reported.
Summary of the invention
In view of the deficiencies of the prior art, the present invention provides a kind of plus hydrogen combinational processing method.This method can add hydrogen simultaneously
Handle refinery gas and production cleaning diesel oil.The utilization efficiency of hydrogen is improved simultaneously under the premise of further increasing diesel product quality
The problem of temperature rise in REFINERY GAS treatment process is efficiently solved, it is overall to reduce equipment investment and reduce operation energy consumption.
Refinery gas of the present invention adds hydrogen combinational processing method, including following content:
(a) diesel raw material oil mixes in molten hydrogen storage equipment with hydrogen with recycle oil, then sequentially enters in diesel oil hydrogenation reactor
Hydrobon catalyst bed and catalyst for hydro-upgrading bed reacted under liquid-phase hydrogenatin operating condition；
(b) enter supplement hydrogenation reaction after the reaction stream that step (a) obtains mixes in molten gas equipment with refinery gas and hydrogen
Hydrogenation catalyst bed in device is reacted under liquid-phase hydrogenatin operating condition；
(c) step (b) hydrogenation reaction effluent is separated into gas phase and liquid phase, continues after isolated gas phase removal hydrogen sulfide point
From the refinery gas after hydrogen, hydrotreating is obtained, isolated liquid phase is fractionated to obtain naphtha and diesel product, part steps
(a) the hydrogenation reaction logistics and/or partial high pressure separator that the hydrogenation reaction effluent and/or part steps (b) obtained obtains
Isolated liquid phase returns in molten hydrogen storage equipment as recycle oil.
In the above method, the diesel raw material oil used may include straight-run diesel oil, catalytic diesel oil, coker gas oil, thermal cracking
The diesel oil distillates such as diesel oil, visbreaking diesel oil, combined diesel oil, coal tar diesel oil distillate, direct liquefying diesel oil of coal, shale oil diesel oil
One or more of.
In the above method, diesel oil hydrogenation operating condition is generally reaction pressure 3.0MPa ~ 16.0MPa, diesel raw material oil body
Product air speed is 0.1h-1~6.0h-1, 180 DEG C ~ 450 DEG C of average reaction temperature, the ratio of recycle oil and diesel raw material oil be 0.2:1 ~
10:1；Preferred operating condition is reaction pressure 4.0MPa ~ 15.0MPa, and diesel raw material oil volume air speed is 0.2h-1~5.0h-1,
200 DEG C ~ 440 DEG C of average reaction temperature, the ratio of recycle oil and diesel raw material oil is 0.5:1 ~ 8:1.
In the above method, supplement Hydroprocessing conditions are generally reaction pressure 3.0MPa ~ 16.0MPa, diesel raw material oil body
Product air speed is 0.3h-1~40.0h-1, 180 DEG C ~ 450 DEG C of average reaction temperature；Preferred operating condition be reaction pressure 4.0MPa ~
15.0MPa, diesel raw material oil volume air speed are 0.5h-1~35.0h-1, 200 DEG C ~ 440 DEG C of average reaction temperature,
In the above method, Hydrobon catalyst hydrogenation active component is one or more of CO, Mo, W, Ni, with oxide
The weight content of meter is 5%~70%, and the carrier of hydrogenation catalyst is generally aluminium oxide, amorphous silicon aluminium, silica, titanium oxide
Deng, while other auxiliary agents, such as P, Si, B, Ti, Zr can be contained.Commercial catalyst can be used, it can also be existing by this field
There is method preparation.Hydrogenation active component is the catalyst of oxidation state, carries out conventional vulcanizing treatment before the use, makes plus hydrogen is living
Property component is converted into sulphided state.Business hydrogenation catalyst mainly has, as Fushun Petrochemical Research Institute (FRIPP) is developed
3936, the hydrogenation catalysts such as CH-20, FF-14, FF-26, FH-5, FH-5A, FH-98, FH-DS, FH-UDS series, FZC-41,
The hydrogenation catalysts such as HR-416, HR-448 of Inst Francais Du Petrole, Uop Inc. HC-P, HC-K UF-210/220 newly developed, AKZO
The hydrogenation catalysts such as KF-752, KF-840, KF-848, KF-901, KF-907 of company.Catalyst for hydro-upgrading is conventional bavin
Oily catalyst for hydro-upgrading, generally using group VIB and/or group VIII metal as active component, group VIB metal is generally Mo
And/or W, group VIII metal are generally Co and/or Ni.The carrier of the catalyst is in aluminium oxide, silicon-containing alumina and molecular sieve
It is one or more, preferably contain molecular sieve, the molecular sieve can be Y type and/or beta molecular sieve.With the weight of catalyst
Meter, group VIB tenor are calculated as 10wt%~35wt% with oxide, group VIII metal content with oxide be calculated as 3wt%~
15wt%, molecular sieve content are 5wt%~40wt%, and alumina content is 10wt%~80wt%, specific surface 100m2/ g~
650m2/ g, Kong Rongwei 0.15mL/g~0.50mL/g.Main catalyst has Fushun Petrochemical Research Institute to develop
3963, FC-18, FC-32, FC-14, FC-20 catalyst etc..For catalyst for hydro-upgrading, it is desirable that have certain plus hydrogen
Active and certain lytic activity, should guarantee alkene and aromatic hydrocarbons in diesel oil distillate plus hydrogen saturation, also require the aromatic hydrocarbons after saturation
The reaction of open loop occurs.Hydrogenation catalyst can be placed in a reactor, can also be placed in more reactors, hydrofinishing
Catalyst is placed in the front of catalyst for hydro-upgrading.The volume ratio of Hydrobon catalyst and catalyst for hydro-upgrading be 20:80 ~
80:20, preferably 25:75 ~ 75:25.
In the above method, step (a) hydrogenator catalyst bed (including Hydrobon catalyst bed and plus hydrogen change
Catalyst bed processed) it is set as multilayer, preferably 2-10 layers, molten gas equipment is arranged in adjacent catalyst bed interlayer；The hydrogen of introducing exists
It is reacted with after reaction stream mixing into next catalyst bed in molten gas equipment.
In the above method, supplementing in hydrogenator can be set a catalyst bed, and multiple catalysis also can be set
Agent bed, preferably 2-8 layer.A catalyst bed is only set if supplementing, liquid-phase hydrogenatin reaction stream is molten in hydrogenator
Enter the top of supplement hydrogenator after mixing in gas device with refinery gas and passes through catalyst bed；If supplementing hydrogenator
It is interior that multiple catalyst beds are set, molten gas equipment is set between bed, enters any adjacent catalyst after refinery gas and hydrogen mixing
The molten gas equipment being arranged between bed, with from the reaction stream of a upper catalyst bed mixing after enter next catalyst bed into
Row reaction.
A kind of preferred embodiment is as follows: diesel oil hydrogenation reactor catalyst bed is set as three layers, and supplement plus hydrogen are anti-
It answers device catalyst bed to be set as two layers, introduces hydrogen between the second catalyst of diesel oil hydrogenation reactor and third catalyst bed
Gas, supplement hydrogenator catalyst bed interlayer introduce hydrogen and refinery gas.
In the above method, diesel raw material oil enters after mixing with recycle oil from the top of diesel oil hydrogenation reactor, molten at this time
The mixture flow for having solved hydrogen downlink can pass through catalyst bed from up to down, and diesel raw material oil can also after mixing with recycle oil
To enter from the bottom of hydrogenator, the mixture flow for having dissolved hydrogen at this time can pass through catalyst bed with bottom-up uplink
Layer.
In the above method, diesel oil hydrogenation reaction effluent has dissolved the mixture flow of refinery gas from supplement hydrogenator
Top enters, and the mixture flow for having dissolved refinery gas at this time downlink can pass through catalyst bed from up to down, and diesel oil hydrogenation is anti-
The mixture flow for answering effluent to dissolve refinery gas can also enter from the bottom of supplement hydrogenator, dissolve refinery at this time
The mixture flow of gas can pass through catalyst bed with bottom-up uplink.
In the above method, a upper catalyst bed or next catalyst bed are with the flow direction of reaction stream
Benchmark, either up flow type or downflow system hydrogenation reaction, the bed first contacted with reaction stream in adjacent bed be it is upper, be followed by
Under touching is.
In the above method, the refinery gas may include one of gases such as dry gas, liquefied gas or several.Gas
Source can be coking, catalytic cracking, thermal cracking, visbreaking etc. reaction one or more of.
In the above method, if hydrogen and refinery gas are introduced during any simultaneously, the hydrogen and refinery gas volume ratio of introducing
For 1:1 ~ 100:1, preferably 1:1 ~ 50:1.
In the above method, hydrogenation reaction effluent separation uses high-pressure separator and/or low pressure separator.The high pressure
Separator is conventional gas-liquid separator.The hydrogenation reaction logistics isolated gas and liquid in high-pressure separator.
The low pressure separator is conventional gas-liquid separator.Isolated liquid is separated in high-low pressure in the high-pressure separator
Isolated gas and liquid in device.
In the above method, the fractionating system for being fractionated use includes stripper and/or fractionating column.In the low pressure separator
Isolated liquid, which is stripped and/or is fractionated in fractionating system, obtains naphtha product and diesel product.
In the above method, gas separator used by gas separates is conventional separator.The high-pressure separator
In in isolated gas and low pressure separator isolated gas mixing and after removing hydrogen sulfide in gas separator
In isolated hydrogen, dry gas and liquefied gas etc., stripper and/or fractionating column are directly entered if having product liquid.
In gas hydrogenation process, because exothermic heat of reaction amount makes greatly the temperature rise of catalyst bed big, lead to hydrogenation reaction temperature
Section is big, not only affects the effect of hydrogenation reaction, but also accelerates the generation of catalyst carbon deposition, reduces the use of catalyst
Period.Hydrogenation reaction is realized by dissolving hydrogen in the oil in diesel oil liquid-phase hydrogenatin modifying process, reaches production cleaning bavin
The purpose of oil product, but dissolve hydrogen be it is excessive, can not react completely, meeting in hydrogenated oil after the reaction was completed
The hydrogen of dissolution usually remaining can dissolve in the 20% ~ 70% of hydrogen, to cause the invalid use of hydrogen, that is, increase energy
Consumption.
The present invention still dissolves a large amount of hydrogen by making full use of diesel oil liquid phase circulation hydrogenation modifying process to generate in oil
A supplement hydrogenator is arranged diesel oil hydrogenation reactor is subsequent, by refinery gas dissolution of raw material in diesel oil hydrogenation in feature again
In reaction stream and enter supplement hydrogenator catalyst bed, completes gas using the hydrogen of dissolution and the atmosphere of catalyst
Hydrogenation reaction, not only solve the problem that gas adds hydrogen temperature rise big, and the hydrogen dissolved in diesel oil is used for gas and adds hydrogen
Reaction reduces hydrogen consumption；Or multiple catalyst beds are arranged in further supplement hydrogenator, it will be in mixed gas
Part dry gas or whole dry gas raw materials and diesel oil hydrogenation generate oil and are mixed into the first catalyst bed, by remaining gas
And/or hydrogen blend mixture enters subsequent catalyst bed, this mainly allows hydrogen consumption low, cuts the dry gas for being easiest to react first
Hydrogenation reaction is carried out, then allows hydrogen to consume slightly higher liquefied gas and is reacted into subsequent catalyst bed, and require supplementation with
It is supplemented into when hydrogen in subsequent catalyst bed entrance；Hydro-upgrading reaction stream continues through supplement hydrofinishing
Catalyst bed, the unsaturated hydrocarbons that hydro-upgrading can be made to generate carry out supplement hydrofining reaction, can save hydro-upgrading
Catalyst for refining after in reactor, or further increase the quality of diesel oil.Combined method aggregate performance is not influence diesel oil
Product quality completes gas hydrogenation process under the premise of further increasing diesel product quality, and it is gentle to obtain diesel product
Body product, and two kinds of technical optimization combinations, the hydrogen for reducing diesel product dissolution reduce hydrogen consumption and energy consumption, Er Qiejie
It has saved equipment investment and has reduced operating cost.
Detailed description of the invention
Fig. 1 is the flow chart of combined hydrogenation method of the present invention.
Wherein: 1- feedstock oil, 2- raw oil pump, 3- recycle oil, 4- hydrogen-dissolving device, the new hydrogen of 5-, 6- refinery gas raw material, 7- diesel oil
Hydrogenator, 8- exhaust valve, 9- diesel oil hydrogenation reaction stream, 10- high-pressure separator, 11- low pressure separator, 12- stripping/point
Evaporate system, 13- stripping gas, 14- naphtha, 15- diesel oil, 16- high-pressure separator gas, 17- low pressure separator gas, 18- gas
Body separator, 19- hydrogen, 20- dry gas, 21- liquefied gas, 22- gas dissolver, 23- supplement hydrogenator, and 24- supplement plus hydrogen are anti-
Answer logistics.
Specific embodiment
The process and effect of combined hydrogenation method of the present invention, but following embodiment are further illustrated below with reference to embodiment
The limitation to the method for the present invention is not constituted.
A kind of combined hydrogenation method specific embodiment of the present invention is as follows: feedstock oil 1 is mixed with recycle oil 3, mixed
Material enters diesel oil hydrogenation reactor 7, diesel oil hydrogenation reaction stream 9 and refinery gas raw material after mixing in hydrogen-dissolving device 4 with hydrogen
Entering supplement hydrogenator 23 after mixing in gas dissolver 22, supplement hydrogenation reaction effluent 9 enters high-pressure separator 10,
Isolated gas 16 and liquid, liquid enter low pressure separator 11 in high-pressure separator 10, separate in low pressure separator 11
Gas 17 and liquid are obtained, the liquid liquid component isolated with gas separator 18 enters stripping/fractionating system after mixing
12, fractionation obtains naphtha 14 and diesel oil 15 under the action of stripping gas 13 in fractionating system, and gas 16 and gas 17 mix
Enter gas separator 18, isolated hydrogen, dry gas and liquefied gas product in gas separator 18 afterwards.Recycle oil 3 can be with
It directly obtains, can also be obtained in the isolated liquid of high-pressure separator 10 from 9.
Concrete condition of the invention is further illustrated below by embodiment.It is developed and is produced using FRIPP
FH-UDS-6/FC-32 catalyst (volume ratio 60:40) has carried out experimental study.
1 diesel raw material main character of table
2 refinery gas raw material main character of table
3 embodiment process conditions of table and major product property
Diesel raw material and refinery gas raw material can be produced directly by the combined hydrogenation method of this technology it can be seen from embodiment
Clean diesel product and clean gas product.
Claims (14)
1. REFINERY GAS combined method, it is characterised in that: including following content:
(a) diesel raw material oil mixes in molten hydrogen storage equipment with hydrogen with recycle oil, then sequentially enters in diesel oil hydrogenation reactor
Hydrobon catalyst bed and catalyst for hydro-upgrading bed reacted under liquid-phase hydrogenatin operating condition；
(b) enter supplement hydrogenation reaction after the reaction stream that step (a) obtains mixes in molten gas equipment with refinery gas and hydrogen
Hydrogenation catalyst bed in device is reacted under liquid-phase hydrogenatin operating condition；
(c) step (b) hydrogenation reaction effluent is separated into gas phase and liquid phase, continues after isolated gas phase removal hydrogen sulfide point
From the refinery gas after hydrogen, hydrotreating is obtained, isolated liquid phase is fractionated to obtain naphtha and diesel product, part steps
(a) the hydrogenation reaction logistics and/or partial high pressure separator that the hydrogenation reaction effluent and/or part steps (b) obtained obtains
Isolated liquid phase returns in molten hydrogen storage equipment as recycle oil.
2. according to the method described in claim 1, it is characterized by: diesel raw material oil is straight-run diesel oil, catalytic diesel oil, coking bavin
Oil, thermal cracking diesel oil, visbreaking diesel oil, combined diesel oil, coal tar diesel oil distillate, direct liquefying diesel oil of coal, shale oil diesel oil
One or more of.
3. according to the method described in claim 1, it is characterized by: diesel oil hydrogenation operating condition be reaction pressure 3.0MPa ~
16.0MPa, diesel raw material oil volume air speed are 0.1h-1~6.0h-1, 180 DEG C ~ 450 DEG C of average reaction temperature, recycle oil and diesel oil
The ratio of feedstock oil is 0.2:1 ~ 10:1.
4. according to the method described in claim 3, it is characterized by: diesel oil hydrogenation operating condition be reaction pressure 4.0MPa ~
15.0MPa, diesel raw material oil volume air speed are 0.2h-1~5.0h-1, 200 DEG C ~ 440 DEG C of average reaction temperature, recycle oil and diesel oil
The ratio of feedstock oil is 0.5:1 ~ 8:1.
5. according to the method described in claim 1, it is characterized by: supplement Hydroprocessing conditions be reaction pressure 3.0MPa ~
16.0MPa, diesel raw material oil volume air speed are 0.3h-1~40.0h-1, 180 DEG C ~ 450 DEG C of average reaction temperature.
6. according to the method described in claim 5, it is characterized by: supplement Hydroprocessing conditions be reaction pressure 4.0MPa ~
15.0MPa, diesel raw material oil volume air speed are 0.5h-1~30.0h-1, 200 DEG C ~ 440 DEG C of average reaction temperature.
7. according to the method described in claim 1, it is characterized by: the Hydrobon catalyst used in diesel oil hydrogenation reactor
It is one or more of CO, Mo, W, Ni with the hydrogenation catalyst hydrogenation active component used in supplement hydrogenator, with oxygen
The weight content of compound meter is 5%~70%, and the carrier of hydrogenation catalyst is aluminium oxide, in amorphous silicon aluminium, silica, titanium oxide
One or more.
8. according to the method described in claim 1, it is characterized by: the catalyst for hydro-upgrading used in diesel oil hydrogenation reactor
Using group VIB and/or group VIII metal as active component, carrier is the aluminium oxide of type containing Y and/or beta molecular sieve, group VIB
Tenor is calculated as 10wt%~35wt% with oxide, and group VIII metal content is calculated as 3wt%~15wt%, molecular sieve with oxide
Content is 5wt%~40wt%.
9. according to the method described in claim 1, it is characterized by: the volume of Hydrobon catalyst and catalyst for hydro-upgrading
Than for 20:80 ~ 80:20.
10. according to the method described in claim 9, it is characterized by: the body of Hydrobon catalyst and catalyst for hydro-upgrading
Product is than being 25:75 ~ 75:25.
11. according to the method described in claim 1, it is characterized by: diesel oil hydrogenation reactor in and/or supplement hydrogenator
Interior 2-10 catalyst bed of setting.
12. according to the method for claim 11, it is characterised in that: three catalyst beds are arranged in diesel oil hydrogenation reactor
Layer, supplement hydrogenator is interior to be arranged two catalyst beds, molten gas equipment is arranged between the bed, hydrogen enters diesel oil hydrogenation
The molten gas equipment of reactor beds interlayer, hydrogen and refinery gas enter the molten gas equipment between supplement hydrogenator bed.
13. according to the method described in claim 1, it is characterized by: the refinery gas be one of dry gas, liquefied gas or
Person is several, and gas source is in one or more of coking, catalytic cracking, thermal cracking, visbreaking reaction.
14. according to claim 1 or method described in 12, it is characterised in that: while when introducing hydrogen and refinery gas, the hydrogen of introducing
Gas and refinery gas volume ratio are 1:1 ~ 100:1.
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101880549A (en) * | 2009-05-06 | 2010-11-10 | 中国石油化工股份有限公司 | Hydrogenation method for liquefied gas fraction |
| CN102268293A (en) * | 2010-06-07 | 2011-12-07 | 中国石油化工集团公司 | Hydrogenation combined process |
| CN104560132A (en) * | 2013-10-29 | 2015-04-29 | 中国石油化工股份有限公司 | Method for hydrotreatment of continuous liquid-phase wax oil |
-
2017
- 2017-11-14 CN CN201711118817.9A patent/CN109777502B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101880549A (en) * | 2009-05-06 | 2010-11-10 | 中国石油化工股份有限公司 | Hydrogenation method for liquefied gas fraction |
| CN102268293A (en) * | 2010-06-07 | 2011-12-07 | 中国石油化工集团公司 | Hydrogenation combined process |
| CN104560132A (en) * | 2013-10-29 | 2015-04-29 | 中国石油化工股份有限公司 | Method for hydrotreatment of continuous liquid-phase wax oil |
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Effective date of registration: 20230908 Address after: 100728 No. 22 North Main Street, Chaoyang District, Beijing, Chaoyangmen Patentee after: CHINA PETROLEUM & CHEMICAL Corp. Patentee after: Sinopec (Dalian) Petrochemical Research Institute Co.,Ltd. Address before: 100728 No. 22 North Main Street, Chaoyang District, Beijing, Chaoyangmen Patentee before: CHINA PETROLEUM & CHEMICAL Corp. Patentee before: DALIAN RESEARCH INSTITUTE OF PETROLEUM AND PETROCHEMICALS, SINOPEC Corp. |