CN203238222U - Liquid phase hydrogenation reaction device with multistage hydrogen dissolving system - Google Patents
Liquid phase hydrogenation reaction device with multistage hydrogen dissolving system Download PDFInfo
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- CN203238222U CN203238222U CN 201320162859 CN201320162859U CN203238222U CN 203238222 U CN203238222 U CN 203238222U CN 201320162859 CN201320162859 CN 201320162859 CN 201320162859 U CN201320162859 U CN 201320162859U CN 203238222 U CN203238222 U CN 203238222U
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- 239000001257 hydrogen Substances 0.000 title claims abstract description 83
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 83
- 239000007791 liquid phase Substances 0.000 title claims abstract description 28
- 238000005984 hydrogenation reaction Methods 0.000 title abstract description 31
- 125000004435 hydrogen atom Chemical class [H]* 0.000 title 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 74
- 238000006243 chemical reaction Methods 0.000 claims abstract description 31
- 238000010438 heat treatment Methods 0.000 claims abstract description 30
- 239000002994 raw material Substances 0.000 claims abstract description 12
- 238000000034 method Methods 0.000 claims description 29
- 239000003054 catalyst Substances 0.000 abstract description 13
- 239000000047 product Substances 0.000 abstract description 11
- 239000007788 liquid Substances 0.000 abstract description 9
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 abstract description 8
- 150000002431 hydrogen Chemical class 0.000 abstract description 7
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 abstract description 4
- 229910021529 ammonia Inorganic materials 0.000 abstract description 4
- 239000006227 byproduct Substances 0.000 abstract description 4
- 239000007789 gas Substances 0.000 abstract description 4
- 229910000037 hydrogen sulfide Inorganic materials 0.000 abstract description 4
- 238000007599 discharging Methods 0.000 abstract description 3
- 239000003921 oil Substances 0.000 description 37
- 239000005864 Sulphur Substances 0.000 description 8
- 239000002283 diesel fuel Substances 0.000 description 8
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 7
- 238000009736 wetting Methods 0.000 description 5
- 238000006477 desulfuration reaction Methods 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 239000012071 phase Substances 0.000 description 4
- 230000023556 desulfurization Effects 0.000 description 3
- 230000007613 environmental effect Effects 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 239000007795 chemical reaction product Substances 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 230000008595 infiltration Effects 0.000 description 2
- 238000001764 infiltration Methods 0.000 description 2
- 230000002262 irrigation Effects 0.000 description 2
- 238000003973 irrigation Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 150000004767 nitrides Chemical class 0.000 description 2
- 150000002897 organic nitrogen compounds Chemical class 0.000 description 2
- 239000002904 solvent Substances 0.000 description 2
- 230000002411 adverse Effects 0.000 description 1
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 1
- 238000004517 catalytic hydrocracking Methods 0.000 description 1
- 238000009903 catalytic hydrogenation reaction Methods 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 230000002860 competitive effect Effects 0.000 description 1
- 230000001627 detrimental effect Effects 0.000 description 1
- 239000000796 flavoring agent Substances 0.000 description 1
- 235000019634 flavors Nutrition 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000011344 liquid material Substances 0.000 description 1
- 239000010687 lubricating oil Substances 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000012188 paraffin wax Substances 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 231100000614 poison Toxicity 0.000 description 1
- 230000007096 poisonous effect Effects 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 230000000452 restraining effect Effects 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000007790 solid phase Substances 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000001993 wax Substances 0.000 description 1
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Abstract
The utility model relates to a liquid phase hydrogenation reaction device with a multi-stage hydrogen dissolving system; the heating furnace raw oil heating pipe is connected with the mixer; n hydrogen heating pipes of the heating furnace, wherein one hydrogen heating pipe is connected with the mixer, and the other n-1 hydrogen heating pipes are respectively connected with n-1 hydrogen-oil mixing components arranged between two adjacent catalyst bed layers in the reactor or between the reactors; the mixer is connected with the uppermost catalyst bed layer or the reactor of the multistage hydrogenation reactor; the outlet of the multistage hydrogenation reactor is connected with the stripping tower; the stripping tower is connected with a raw material oil pipe or a product tank; the multistage hydrogenation reactor is provided with an exhaust pipe, and the exhaust pipe is provided with a pressure control valve connected with a pressure gauge; a tail gas discharge pipe is arranged between two adjacent catalyst bed layers or reactors, and each pipe is provided with a liquid level control valve connected with a liquid level meter; the device has the functions of catalyzing hydrogenation reaction and discharging reaction byproducts, namely hydrogen sulfide and ammonia out of a reaction system, and the hydrogenation reaction efficiency is high.
Description
Technical field
The present invention relates to a kind of liquid-phase hydrogenatin reaction unit with multistage molten hydrogen system, relate in particular to the reaction unit that a kind of product circulation liquid-phase hydrogenatin is processed.
Background technology
Along with people's environmental consciousness constantly strengthens, a lot of countries limit the sulphur contents of diesel oil by environmental legislation, make it reach very low level (10～15 μ g/g), to reduce the discharging of obnoxious flavour, improve Air quality.The U.S. made the sulphur content in the diesel oil be reduced to 15 μ g/g in 2006.Germany is reduced to 10 μ g/g in the January, 2003 with sulphur content.European Union other countries and Japan were reduced to 10 μ g/g in 2008 with sulphur content.China city motor diesel oil standard GB/T 19147-2009 formulates with reference to European III class standard, and its sulphur content requires less than 350 μ g/g.The diesel oil sulphur content requires less than 10 μ g/g in the automobile-used petrol and diesel oil discharge index of five-stage of national environmental protection section issue.
World market diesel oil demand is in continuous growth, yet high-grade stock oil supply is but reducing.How utilizing low-grade stock oil to produce ultra-low-sulphur diesel to satisfy growing demand, is the very large challenge that refinery has to face.Be to cope with challenges, need on the one hand to solve a gordian technique difficult problem, newly-built hydrogenation unit carries out the deep hydrodesulfurizationof of diesel oil; Need again on the one hand in addition reduce the risk and overlapping investment to ensure economic benefit.In traditional trickle bed hydrogenation technique, hydrogen need to be delivered to liquid phase from gas phase, and then dissolved hydrogen and sulfocompound react in the active centre of catalyzer, thereby reaches the desulfurization purpose.In this process, needed amounts of hydrogen is far longer than the amounts of hydrogen that hydrogenation reaction consumes.This is because on the one hand, hydrogenation reaction is a strong exothermal reaction, in order to control temperature of reaction, needs a large amount of hydrogen and stock oil to take away reaction heat by beds; On the one hand, in the reaction of gas-liquid-solid three-phase, keep higher hydrogen dividing potential drop and be conducive to hydrogenation reaction in addition, suppress coke and generate the extending catalyst life-span.In addition, the hydrogen of participation reaction is transported to participation reaction in the reactor after by circulating hydrogen compressor it being improved pressure again.Circulating hydrogen compressor is as the key equipment of hydrogenation process, and investment and process cost are higher.In order to cancel recycle hydrogen and circulating hydrogen compressor, reduce the cost of investment of device, the liquid-phase hydrogenatin technology has been carried out, in the liquid phase circulation hydrogenation technique, hydrogen and the pre-mixing of stock oil elder generation are dissolved in the stock oil hydrogen, enter reactor again and react, required hydrogen from the hydrogen of dissolving, and need not additionally to fill into cold hydrogen fully in the reaction process.It is smaller that the liquid phase circulation hydrogenation technique has reactor, cost of investment is low, the advantages such as the easy control of temperature of reaction, but, also there is a problem in the liquid phase circulation hydrogenation, namely in order to satisfy needed amounts of hydrogen in the hydrogenation process, need to or additionally add solvent with a large amount of turning oil and dissolve hydrogen, cause hydrogenation efficiency to reduce.
The speed of reaction that generally contains raw material hydrogenating desulfurization in the trickle bed hydrogenator of simple sulfide has the relation except the concentration with organic sulfide, also is subjected to wetting situation, the organic nitrogen compound in the reactor assembly and the H of catalyzer
2The impact of the factors such as S concentration.The wetting factor of catalyzer is by a kind of tolerance of liquid reactants institute infiltration degree to catalyst surface under hydrogenation conditions.The infiltration degree of catalyzer is higher, the wetting factor of catalyzer is just higher, that is to say that the effective rate of utilization of catalyzer is higher.Under the condition that the factors such as catalyzer are determined, the principal element that affects the catalyst irrigation factor is the flow velocity of liquid in the reactor, and the ratio (hydrogen-oil ratio) of gas and flow rate of liquid.It is generally acknowledged, flow rate of liquid increases and strengthens the catalyst irrigation effect, and conventional hydrogenation technique adopts considerably beyond the required large hydrogen-oil ratio of reaction more, thereby has reduced the wetting effect of catalyzer, and the wetting factor is had adverse influence.In addition, the investment of hydrogen recycle link accounts for the large percentage of whole process cost in the oil refining process.
Organic nitrogen compound is the poisonous substance of hydrogenation catalyst, and hydrodenitrification, hydrogenating desulfurization and hydrogenation dearomatization reaction are had obvious restraining effect.This supression effect mainly is because some nitride and the intermediate reaction product of most of nitride and the hydrogenation reaction active centre of catalyzer have very strong sorptive power, has restrained the carrying out of other hydrogenation reactions from the angle of competitive adsorption.And will greatly dilute foreign matter content in the raw material by hydrogenation products circulation, be conducive to bring into play the performance of catalyzer.
US Patent No. 20060144756A1 discloses a kind of two-phase hydrogenation Controlling System method and apparatus.In continuous liquid-phase hydrogenatin process, cancelled recycle hydrogen, the needed hydrogen of hydrogenation reaction all comes from the hydrogen of liquid phase dissolved, does not need extra hydrogen.But it need to dissolve hydrogen with hydrogen solubility larger solvent or thinner, affects follow-up hydrogenation efficiency.
US6213835, US6428686, CN200680018017.3 etc. disclose a kind of hydrogenation technique that dissolves in advance hydrogen, by amount of liquid or the air pressure in the amounts of hydrogen control reactor in the control liquid feeding.But it does not solve the H that will produce fully in the hydrofining reaction process
2S, NH
3Deng the problem that detrimental impurity removes, cause it constantly in reactor, to accumulate, greatly reduce reaction efficiency, also can't effectively process sulphur, raw material that nitrogen content is higher, above-mentioned document is reactor openly also
Concrete structure.
The utility model content
The purpose of this utility model provides a kind of liquid-phase hydrogenatin reaction unit with multistage molten hydrogen system.
Liquid-phase hydrogenatin reaction unit with multistage molten hydrogen system described in the utility model is comprised of process furnace, multistage hydrogenator, stripping tower and mixing tank; Process furnace is provided with a stock oil heating tube, and stock oil heating tube entrance is connected with the raw material oil pipe, and the outlet of stock oil heating tube is connected with mixer entrance; Process furnace is provided with n root hydrogen heating tube, and hydrogen heating tube entrance is connected with hydrogen pipe; A hydrogen heating tube outlet is connected with mixer entrance, and all the other n-1 root hydrogen heating tube outlets are connected with the oily hybrid component entrance of n-1 hydrogen in being arranged on reactor by n-1 reactor bed or the entrance between the reactor that is arranged on the multistage hydrogenator respectively; Multistage hydrogenator is provided with n beds or reactor, and hydrogen oil hybrid component is arranged between two adjacent beds or reactor; Mixer outlet is connected with multistage hydrogenator the superiors' beds or reactor inlet; The outlet line that multistage hydrogenator is arranged on the bottom is connected with the entrance that is positioned at stripping tower top by generating oil pipeline, generates on the oil pipeline and is connected with the level control valve D that is connected with liquidometer; The outlet that stripping tower is positioned at the bottom is connected with the raw material oil pipe with circulating pipe by recycle pump or the products pot connection; Multistage hydrogenator top is provided with vapor pipe, and vapor pipe is provided with the pressure controlled valve that is connected with tensimeter; Be provided with exhaust emission tube between two adjacent beds of multistage hydrogenator or the reactor, be provided with the level control valve that is connected with liquidometer on the every pipe.
The part circulation that mixes the liquid material of hydrogen through stripping tower is mixed into liquid phase material with fresh feed oil, and liquid phase material enters the process furnace heating; Hydrogen is divided into the n road and enters the process furnace heating, perhaps is divided into the n road after the process furnace heating, and n equals the quantity of reactor catalyst bed or the quantity of staged reactor.Wherein one road hydrogen and oil product mix in mixing tank, carry out the molten hydrogen of the first step, all the other (n-1) road hydrogen enter the oil of hydrogen in reactor hybrid component by the entrance between the reactor catalyst bed to be mixed with mixture behind the upper catalyst bed reaction, carry out the molten hydrogen in the second stage, stripping goes out byproduct of reaction hydrogen sulfide and ammonia simultaneously, every many beds or a reactor just increase the molten hydrogen of one-level, in reactor head the reaction pressure Controlling System is set, at every section reactor exhaust system is set, the liquid level of every section reactor by controlling next section generation gas and the discharging of unnecessary hydrogen realize.Reaction product enters stripping tower, and hydrogen oil mixing tank is set in the stripping tower, and product can go out by product hydrogen sulfide and ammonia by stripping, increases simultaneously dissolve hydrogen capacity, and a stripping tower oil product part out enters products pot, a part of recirculation.
Liquid-phase hydrogenatin reaction unit with multistage molten hydrogen system described in the utility model is 3～5 by the number of reactor catalyst bed or the number n of staged reactor.
In the utility model method, the liquid phase stream behind the dissolved hydrogen enters reactor from liquid phase circulation hydrogenator top, flows out from reactor lower part; Perhaps liquid phase stream enters reactor from liquid phase circulation hydrogenator bottom, flows out from reactor top.
In the utility model method, hydrogen oil mixing tank or hydrogen oil hybrid component are set in the stripping tower.
A kind of liquid-phase hydrogenatin reaction unit with multistage molten hydrogen system described in the utility model is the two-phase hydrogenation reaction of carrying out in fixed-bed reactor, and reacting needed hydrogen is provided by the excess hydrogen of dissolving in the stock oil.
The hydrogenator that the utility model adopts has simultaneously catalytic hydrogenation reaction and byproduct of reaction hydrogen sulfide and ammonia is discharged the effect of reactive system function, and what contact with solid-phase catalyst is liquid phase reacting material, thereby has improved hydrogenation reaction efficient.
The utility model be mainly used in the poor ignition quality fuel component deep desulfuration, denitrogenation, take off aromatic hydrocarbons, produce clean diesel, also can be used for the hydrofining production high-quality oil products such as petroleum naphtha, boat coal, lubricating oil, paraffin, and be used for wax oil raw material mild hydrocracking production high-quality cleaning boat coal, diesel oil technological process.
Description of drawings
Fig. 1 is the liquid-phase hydrogenatin reaction unit structural representation with multistage molten hydrogen system.
Among the figure: 1-raw material oil pipe, 2-circulating pipe, 3-hydrogen pipe, 4-process furnace, the 5-mixing tank, the multistage hydrogenator of 6-, 7-pressure controlled valve, 8 vapor pipes, 9-level control valve A, 10-level control valve B, 11-level control valve C, 12-level control valve D, 13-exhaust emission tube A, 14-exhaust emission tube B, 15-exhaust emission tube C, 16-generates oil pipeline, 17-stripping tower, 18-exhaust emission tube E, 19-stripping tracheae, 20-recycle pump, 21-products pot
Embodiment
Liquid-phase hydrogenatin reaction unit with multistage molten hydrogen system described in the utility model is comprised of process furnace 4, multistage hydrogenator 6, stripping tower 17 and mixing tank 5; Process furnace 4 is provided with a stock oil heating tube, and stock oil heating tube entrance is connected with raw material oil pipe 1, and the outlet of stock oil heating tube is connected with mixing tank 5 entrances; Process furnace 4 is provided with n root hydrogen heating tube, and hydrogen heating tube entrance is connected with hydrogen pipe 3; A hydrogen heating tube outlet is connected with mixing tank 5 entrances, and all the other n-1 root hydrogen heating tube outlets are connected with the oily hybrid component entrance of n-1 hydrogen in being arranged on reactor by n-1 reactor bed or the entrance between the reactor that is arranged on the multistage hydrogenator 6 respectively; Multistage hydrogenator 6 is provided with n beds or reactor, and hydrogen oil hybrid component is arranged between two adjacent beds or reactor; Mixing tank 5 outlets are connected with multistage hydrogenator 6 the superiors' beds or reactor inlet; The outlet line that multistage hydrogenator 6 is arranged on the bottom is connected with the entrance that is positioned at stripping tower 17 tops by generating oil pipeline 16, generates on the oil pipeline and is connected with the level control valve D12 that is connected with liquidometer; The outlet that stripping tower 17 is positioned at the bottom is connected with circulating pipe by recycle pump 20 and is connected or products pot 21 connections with raw material oil pipe 1; Multistage hydrogenator 6 tops are provided with vapor pipe 8, and vapor pipe is provided with the pressure controlled valve 7 that is connected with tensimeter; Be provided with exhaust emission tube A13, exhaust emission tube B14, exhaust emission tube C15 between two adjacent beds of multistage hydrogenator 6 or the reactor, be provided with level control valve A9, level control valve B10, the level control valve C11 that is connected with liquidometer on the every pipe, stripping tower 17 tops are provided with exhaust emission tube E18, and the bottom is provided with stripping tracheae 19.
Claims (3)
1. the liquid-phase hydrogenatin reaction unit with multistage molten hydrogen system is comprised of process furnace, multistage hydrogenator, stripping tower and mixing tank; It is characterized in that: process furnace is provided with a stock oil heating tube, and stock oil heating tube entrance is connected with the raw material oil pipe, and the outlet of stock oil heating tube is connected with mixer entrance; Process furnace is provided with n root hydrogen heating tube, and hydrogen heating tube entrance is connected with hydrogen pipe; A hydrogen heating tube outlet is connected with mixer entrance, and all the other n-1 root hydrogen heating tube outlets are connected with the oily hybrid component entrance of n-1 hydrogen in being arranged on reactor by n-1 reactor bed or the entrance between the reactor that is arranged on the multistage hydrogenator respectively; Multistage hydrogenator is provided with n beds or reactor, and hydrogen oil hybrid component is arranged between two adjacent beds or reactor; Mixer outlet is connected with multistage hydrogenator the superiors' beds or reactor inlet; The outlet line that multistage hydrogenator is arranged on the bottom is connected with the entrance that is positioned at stripping tower top by generating oil pipeline, generates on the oil pipeline and is connected with the level control valve D that is connected with liquidometer; The outlet that stripping tower is positioned at the bottom is connected with the raw material oil pipe with circulating pipe by recycle pump or the products pot connection; Multistage hydrogenator top is provided with vapor pipe, and vapor pipe is provided with the pressure controlled valve that is connected with tensimeter; Be provided with exhaust emission tube between two adjacent beds of multistage hydrogenator or the reactor, be provided with the level control valve that is connected with liquidometer on the every pipe.
2. according to the liquid-phase hydrogenatin reaction unit with multistage molten hydrogen system claimed in claim 1, it is characterized in that: n is 3～5.
3. according to the liquid-phase hydrogenatin reaction unit with multistage molten hydrogen system claimed in claim 1, it is characterized in that: hydrogen oil mixing tank or hydrogen oil hybrid component are set in the stripping tower.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201320162859 CN203238222U (en) | 2013-04-03 | 2013-04-03 | Liquid phase hydrogenation reaction device with multistage hydrogen dissolving system |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201320162859 CN203238222U (en) | 2013-04-03 | 2013-04-03 | Liquid phase hydrogenation reaction device with multistage hydrogen dissolving system |
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| CN203238222U true CN203238222U (en) | 2013-10-16 |
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| CN 201320162859 Expired - Fee Related CN203238222U (en) | 2013-04-03 | 2013-04-03 | Liquid phase hydrogenation reaction device with multistage hydrogen dissolving system |
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105524657A (en) * | 2014-09-29 | 2016-04-27 | 中国石油化工股份有限公司 | Method for hydrogenation of distillate oil via fluidized bed |
| CN105861046A (en) * | 2015-01-23 | 2016-08-17 | 中国石油化工股份有限公司 | Diesel oil ultra-deep desulfurization system |
| CN106701173A (en) * | 2015-11-18 | 2017-05-24 | 中国石油天然气股份有限公司 | liquid phase hydrogenation device and method |
| CN106701179A (en) * | 2015-11-18 | 2017-05-24 | 中国石油天然气股份有限公司 | Liquid phase hydrogenation device and method |
| CN106701180A (en) * | 2015-11-18 | 2017-05-24 | 中国石油天然气股份有限公司 | Liquid phase hydrogenation device and method |
| CN106701174B (en) * | 2015-11-18 | 2018-08-14 | 中国石油天然气股份有限公司 | liquid phase hydrogenation device and method |
| CN112093776A (en) * | 2020-09-18 | 2020-12-18 | 青岛海望能源科技有限公司 | Continuous organic liquid hydrogenation system and method with optimally-arranged catalyst |
-
2013
- 2013-04-03 CN CN 201320162859 patent/CN203238222U/en not_active Expired - Fee Related
Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105524657A (en) * | 2014-09-29 | 2016-04-27 | 中国石油化工股份有限公司 | Method for hydrogenation of distillate oil via fluidized bed |
| CN105524657B (en) * | 2014-09-29 | 2017-03-29 | 中国石油化工股份有限公司 | A kind of fraction oil boiling bed hydrogenation method |
| CN105861046A (en) * | 2015-01-23 | 2016-08-17 | 中国石油化工股份有限公司 | Diesel oil ultra-deep desulfurization system |
| CN105861046B (en) * | 2015-01-23 | 2018-06-19 | 中国石油化工股份有限公司 | A kind of Ultra-deep Desulfurization of Diesel Fuels system |
| CN106701173A (en) * | 2015-11-18 | 2017-05-24 | 中国石油天然气股份有限公司 | liquid phase hydrogenation device and method |
| CN106701179A (en) * | 2015-11-18 | 2017-05-24 | 中国石油天然气股份有限公司 | Liquid phase hydrogenation device and method |
| CN106701180A (en) * | 2015-11-18 | 2017-05-24 | 中国石油天然气股份有限公司 | Liquid phase hydrogenation device and method |
| CN106701173B (en) * | 2015-11-18 | 2018-08-10 | 中国石油天然气股份有限公司 | liquid phase hydrogenation device and method |
| CN106701174B (en) * | 2015-11-18 | 2018-08-14 | 中国石油天然气股份有限公司 | liquid phase hydrogenation device and method |
| CN106701180B (en) * | 2015-11-18 | 2018-09-04 | 中国石油天然气股份有限公司 | liquid phase hydrogenation device and method |
| CN106701179B (en) * | 2015-11-18 | 2018-09-04 | 中国石油天然气股份有限公司 | liquid phase hydrogenation device and method |
| CN112093776A (en) * | 2020-09-18 | 2020-12-18 | 青岛海望能源科技有限公司 | Continuous organic liquid hydrogenation system and method with optimally-arranged catalyst |
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