CN109777505A - REFINERY GAS combined method - Google Patents
REFINERY GAS combined method Download PDFInfo
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- CN109777505A CN109777505A CN201711118869.6A CN201711118869A CN109777505A CN 109777505 A CN109777505 A CN 109777505A CN 201711118869 A CN201711118869 A CN 201711118869A CN 109777505 A CN109777505 A CN 109777505A
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Abstract
The present invention discloses a kind of REFINERY GAS combined method, including following content :(a) diesel raw material oil mixes in molten hydrogen storage equipment with hydrogen with recycle oil, is reacted under liquid-phase hydrogenatin operating condition subsequently into the hydrogenation catalyst bed in diesel oil hydrogenation reactor；(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 diesel product, 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 techniques of oil Refining Technologies, are related to a kind of REFINERY GAS combined method, relate in particular to one
The combined hydrogenation method of the processing of kind REFINERY GAS 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..
Diesel oil hydrogenation technology is to improve the most important means of diesel product quality, and liquid phase diesel oil hydrogenation technology can be substantially
Degree reaches the requirement of cleaning diesel production in the case where reducing energy consumption.US6213835 and US6428686 discloses a kind of molten in advance
The hydrogenation technique of hydrogen.CN201110274695.9 discloses a kind of method of full liquid-phase hydrogenatin production cleaning diesel oil.
CN201110192784.9 discloses a kind of Diesel oil liquid phase hydrogenation.These methods be all hydrogen is dissolved in diesel raw material into
In addition row hydrogenation reaction is directly handled after separation there is no utilizing to the remaining hydrogen of reaction.
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 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 combined hydrogenation method.This method being capable of hydrotreating simultaneously
Refinery gas and production cleaning diesel oil.The utilization efficiency of hydrogen and effective is improved under the premise of further increasing diesel product quality
Solve the problem of temperature rise in REFINERY GAS treatment process, it is overall to reduce equipment investment and reduce operation energy consumption.
REFINERY GAS combined method of the present invention, including following content:
(a) diesel raw material oil mixes in molten hydrogen storage equipment with hydrogen with recycle oil, subsequently into adding in diesel oil hydrogenation reactor
Hydrogen catalyst bed is 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-1~30.0h-1, 200 DEG C ~ 440 DEG C of average reaction temperature,
In the above method, the hydrogenation catalyst that is used in liquid phase hydrogenation reactor and used in supplement hydrogenator plus hydrogen urge
Agent can be to be same, can not also be identical.Hydrogenation active component is in CO, Mo, W, Ni in used hydrogenation catalyst
One or more, weight content in terms of oxide is 5%~70%, and the carrier of hydrogenation catalyst is generally aluminium oxide, without fixed
Type sial, silica, titanium oxide etc., while other auxiliary agents, such as P, Si, B, Ti, Zr can be contained.Commercial catalyst can be used
Agent can also be prepared by this field existing method.Hydrogenation active component is the catalyst of oxidation state, is carried out before the use conventional
Vulcanizing treatment, so that hydrogenation active component is converted into sulphided state.Business hydrogenation catalyst mainly has, such as Fushun petrochemical industry research
Institute (FRIPP) develop 3936, CH-20, FF-14, FF-26, FH-5, FH-5A, FH-98, FH-DS, FH-UDS series,
The hydrogenation catalysts such as FZC-41, the hydrogenation catalysts such as HR-416, HR-448 of Inst Francais Du Petrole, Uop Inc. HC-P newly developed,
The hydrogenation catalysts such as KF-752, KF-840, KF-848, KF-901, KF-907 of HC-K UF-210/220, AKZO company.
In the above method, step (a) hydrogenator catalyst bed is set as multilayer, and preferably 2-8 layers, adjacent catalyst
Molten gas equipment is set between bed；The hydrogen of introducing in molten gas equipment with reaction stream mixing after enter next catalyst bed into
Row reaction.
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 technique, is reached production cleaning diesel oil and is produced
The purpose of product, but dissolve hydrogen be it is excessive, can not react, can be dissolved in hydrogenated oil after the reaction was completed completely
Hydrogen, 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 by make full use of diesel oil liquid phase circulation hydrogenation technique generate oil in still dissolve a large amount of hydrogen the characteristics of,
A supplement hydrogenator is set again diesel oil hydrogenation reactor is subsequent, by refinery gas dissolution of raw material in diesel oil hydrogenation reactant
In stream and enter supplement hydrogenator catalyst bed, using dissolution hydrogen and catalyst atmosphere complete gas plus hydrogen
Reaction, not only solves the problem that gas adds hydrogen temperature rise big, and the hydrogen dissolved in diesel oil is used for gas hydrogenation reaction, drops
Low hydrogen consumption；Or multiple catalyst beds are arranged in further supplement hydrogenator, and the part in mixed gas is done
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
Gas blend mixture enters subsequent catalyst bed, this mainly allows hydrogen consumption low, cuts the dry gas for being easiest to react and is added first
Then hydrogen reaction allows hydrogen to consume slightly higher liquefied gas and is reacted into subsequent catalyst bed, and requires supplementation with hydrogen
When be supplemented into subsequent catalyst bed entrance.Combined method aggregate performance be do not influence diesel product quality or
Gas hydrogenation process is completed under the premise of further increasing diesel product quality, obtains diesel product and gas products, and
Two kinds of technical optimization combinations, the hydrogen for reducing diesel product dissolution reduces hydrogen consumption and energy consumption, and saves equipment throwing
Money and reduction 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, the refinery 6-
Gas raw material, 7- diesel oil hydrogenation reactor, 8- exhaust valve, 9- diesel oil hydrogenation reaction stream, 10- high-pressure separator, the separation of 11- low pressure
Device, 12- stripping/fractionating system, 13- stripping gas, 14- naphtha, 15- diesel oil, 16- high-pressure separator gas, the separation of 17- low pressure
Device gas, 18- gas separator, 19- hydrogen, 20- dry gas, 21- liquefied gas, 22- gas dissolver, 23- supplement hydrogenator,
24- supplements hydrogenation reaction 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-5/ FH-UDS-6 combination catalyst system 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 (11)
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, subsequently into adding in diesel oil hydrogenation reactor
Hydrogen catalyst bed is 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 hydrogenation catalyst and benefit that are used in diesel oil hydrogenation reactor
Filling the hydrogenation catalyst hydrogenation active component used in hydrogenator 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 aluminium oxide, amorphous silicon aluminium, silica, one in titanium oxide
Kind is several.
8. according to the method described in claim 1, it is characterized by: diesel oil hydrogenation reactor in and/or supplement hydrogenator
Interior 1-8 catalyst bed of setting.
9. according to the method described in claim 8, it is characterized by: diesel oil hydrogenation reactor in be arranged three catalyst beds,
It supplements and two catalyst beds is set in hydrogenator, molten gas equipment is set between the bed, it is anti-that hydrogen enters diesel oil hydrogenation
The molten gas equipment between device bed is answered, hydrogen and refinery gas enter the molten gas equipment between supplement hydrogenator bed.
10. 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.
11. according to claim 1 or method described in 9, 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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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP4183480A4 (en) * | 2020-07-16 | 2024-04-03 | Nanjing Yanchang Reaction Technology Research Institute Co., Ltd | Micro-interface reaction system and method for diesel hydrogenation |
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