CN202063881U - Liquid-phase hydrogenation reactor - Google Patents
Liquid-phase hydrogenation reactor Download PDFInfo
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- CN202063881U CN202063881U CN2011201040690U CN201120104069U CN202063881U CN 202063881 U CN202063881 U CN 202063881U CN 2011201040690 U CN2011201040690 U CN 2011201040690U CN 201120104069 U CN201120104069 U CN 201120104069U CN 202063881 U CN202063881 U CN 202063881U
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- reactor
- mixing tank
- hydrogen
- liquid phase
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- 238000005984 hydrogenation reaction Methods 0.000 title claims abstract description 50
- 239000007791 liquid phase Substances 0.000 title claims abstract description 36
- 239000001257 hydrogen Substances 0.000 claims abstract description 84
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 84
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 75
- 238000002156 mixing Methods 0.000 claims abstract description 71
- 239000000203 mixture Substances 0.000 claims abstract description 24
- 239000007789 gas Substances 0.000 claims abstract description 21
- 239000003054 catalyst Substances 0.000 claims description 8
- 239000011229 interlayer Substances 0.000 claims description 5
- 238000011049 filling Methods 0.000 claims description 2
- 238000006243 chemical reaction Methods 0.000 abstract description 25
- 239000012071 phase Substances 0.000 abstract description 6
- 239000003921 oil Substances 0.000 description 50
- 239000004215 Carbon black (E152) Substances 0.000 description 14
- 229930195733 hydrocarbon Natural products 0.000 description 14
- 150000002430 hydrocarbons Chemical class 0.000 description 14
- 239000000047 product Substances 0.000 description 12
- 238000005516 engineering process Methods 0.000 description 9
- 150000002431 hydrogen Chemical class 0.000 description 9
- 239000007788 liquid Substances 0.000 description 9
- 238000000034 method Methods 0.000 description 9
- 239000003795 chemical substances by application Substances 0.000 description 7
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 6
- 239000005864 Sulphur Substances 0.000 description 5
- 230000008569 process Effects 0.000 description 5
- 239000002994 raw material Substances 0.000 description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- 239000000446 fuel Substances 0.000 description 4
- 238000004517 catalytic hydrocracking Methods 0.000 description 3
- 238000006477 desulfuration reaction Methods 0.000 description 3
- 230000023556 desulfurization Effects 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 239000012535 impurity Substances 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 238000012546 transfer Methods 0.000 description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 230000003197 catalytic effect Effects 0.000 description 2
- 239000000571 coke Substances 0.000 description 2
- 238000006482 condensation reaction Methods 0.000 description 2
- 238000005336 cracking Methods 0.000 description 2
- 239000010779 crude oil Substances 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 230000018109 developmental process Effects 0.000 description 2
- 239000002283 diesel fuel Substances 0.000 description 2
- 239000000295 fuel oil Substances 0.000 description 2
- 230000006872 improvement Effects 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 239000003208 petroleum Substances 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 239000000376 reactant Substances 0.000 description 2
- 238000007670 refining Methods 0.000 description 2
- 230000004044 response Effects 0.000 description 2
- 229910052717 sulfur Inorganic materials 0.000 description 2
- 239000011593 sulfur Substances 0.000 description 2
- 230000009466 transformation Effects 0.000 description 2
- CIWBSHSKHKDKBQ-JLAZNSOCSA-N Ascorbic acid Chemical compound OC[C@H](O)[C@H]1OC(=O)C(O)=C1O CIWBSHSKHKDKBQ-JLAZNSOCSA-N 0.000 description 1
- PFRUBEOIWWEFOL-UHFFFAOYSA-N [N].[S] Chemical compound [N].[S] PFRUBEOIWWEFOL-UHFFFAOYSA-N 0.000 description 1
- 150000001336 alkenes Chemical class 0.000 description 1
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 230000033228 biological regulation Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000004523 catalytic cracking Methods 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000003350 kerosene Substances 0.000 description 1
- 239000010687 lubricating oil Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000003209 petroleum derivative Substances 0.000 description 1
- 238000005191 phase separation Methods 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000003079 shale oil Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000007790 solid phase Substances 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The utility model discloses a liquid-phase hydrogenation reactor. A mixing device is arranged in a seal head of the top part of the reactor; the mixing device is provided with a mixed oil inlet, a hydrogen inlet, a dissolved hydrogen mixture outlet and a gas outlet; and the dissolved hydrogen mixture outlet of the mixing device is inserted into liquid phase of the reactor. The mixing device can be used for effectively increasing the contact surface between a gas phase and the liquid phase and has simple structure; and hydrogen is dissolved in mixed oil to promote the reaction, thereby greatly increasing the hydrogenation efficiency of the hydrogen.
Description
Technical field
The present invention relates to the hydrocarbon oil hydrogenation technology, particularly a kind of liquid phase hydrogenation reactor.
Background technology
The sustainable development of world economy and the increasingly stringent of environmental regulation need to produce a large amount of light clean fuels at present, and these all require existing oil Refining Technologies is improved, and produce satisfactory product with minimum cost.Along with the worsening shortages of crude resources and heaviness, poor qualityization development, catalytic cracking and coking become the important means of producing the light Fuel product, but the quality product that these two kinds of technologies obtain generally is difficult to the quality index requirement that reaches strict.In the light Fuel quality product system, sulphur content is most important index, how to reduce sulphur content in the petroleum products and be one of most significant problems that current petroleum chemical industry faces, the cetane value of diesel product receives publicity always in addition, and its specification requirement is also more and more stricter.At present, be that the main purpose hydrogenation technique has obtained widespread use in Clean Fuel Production with desulfurization and upgrading.
Hydrogen addition technology is to improve one of hydrocarbon ils quality technology commonly used, the crude oil that is tending towards higher sulfur content along with the global crude oil market supply, the refinery need process the higher hydrocarbon ils inferior of sulfur-bearing, sulphur, nitrogen, oxygen and metal impurities are removed in refining process, change its quality by the molecular structure that changes hydrocarbon ils, thereby make various products satisfy code requirement.The hydrogen that in fact the hydrocarbon oil hydrogenation process participates in reacting only is useful on the hydrogen of chemical hydrogen consumption, and traditional trickle-bed reactor hydrogen addition technology, need excessive hydrogen and exist, make that the volume ratio of reactor is bigger, and keep the exess of H2 gas and need use circulating hydrogen compressor.
Hydrogen need be delivered to liquid phase from gas phase in traditional hydrogenation technique, and co-absorbed is reacted under the effect of catalyst active center on the surface of catalyzer then.Because hydrogenation reaction is a strong exothermal reaction, in order to keep temperature of reaction, utilize a large amount of hydrogen and stock oil to take away the heat that reaction produces by beds, and the hydrogen of actual needs (chemical hydrogen consumption) is fewer in hydrogenation process, do not participate in the hydrogen of reaction, be recycled to hydrogenator and continue to participate in reaction; It is to keep the hydrogen dividing potential drop of hydrocarbon oil hydrogenation reaction that tradition hydrocarbon oil hydrogenation technology adopts another major cause of excessive hydrogen, keeps higher hydrogen branch and is pressed in and helps hydrofining and hydrocracking reaction on the thermodynamics, suppresses to generate the condensation reaction of coke.
The hydrogen of participating in reaction is not elevated to the required pressure of reaction by circulating hydrogen compressor with its pressure and delivers to reactor continuation participation hydrogenation reaction by separator and liquid phase separation and after removing impurity.The hydrogen pressurize that the effect of circulating hydrogen compressor will not participate in hydrogenation reaction exactly recycles it, so the circulating hydrogen compressor becomes imperative equipment in existing hydrogen addition technology, is called the heart of hydrogenation unit in the industry.
Be the gas, liquid, solid three-phase in traditional fixed bed hydrogenation reactor and deposit that gas phase is the steam of hydrogen and hydrocarbon raw material, liquid phase is the hydrocarbon raw material of vaporization not, and solid phase is a catalyzer.Gas-liquid two-phase is to pass through beds with the form of drip, therefore also claims trickle-bed reactor.
In trickle-bed reactor, in order to strengthen the mass transfer dynamics, the volume ratio of hydrogen and stock oil is generally 50～2000: 1, therefore the hydrogenator design is bigger, and the actual stock oil that reacts of participating in is relevant with liquid hourly space velocity, air speed has reflected the processing power of device, and bigger air speed operation is adopted in industrial hope, but air speed is subjected to the restriction of speed of response.Air speed is unusual at 0.5～10h according to catalyst activity, feedstock property, reaction depth
-1Between the fluctuation.The unifining process of industrial application can improve alkene saturation exponent, hydrogenating desulfurization rate and hydrodenitrification rate at certain temperature of reaction condition decline low-speed at present.Under hydrocracking condition, it is little to total transformation efficiency influence to improve air speed, but the decline of the light constituent content in the reaction product is more.
The purpose that adopts the exess of H2 gas is to strengthen mass transfer and take away a large amount of heats that produce because of hydrogenation reaction, circulating hydrogen compressor is as the heart of hydrogenation process, investment and process cost are all higher, in order to cancel circulating hydrogen compressor, people begin to consider to utilize hydrogen supply agent to provide hydrogen source for the hydrocarbon oil hydrogenation process, USP4698147 discloses and has utilized hydrogen supply agent to reduce the residence time, and reaction back hydrogen supply agent utilizes hydrogen to regenerate, and recycles after the regeneration.In order to strengthen cracking reaction, USP4857168 discloses and has utilized hydrogen supply agent and hydrogen to provide the heavy-oil hydrogenation cracking method of hydrogen source for heavy-oil hydrogenation, and hydrogen supply agent mainly works to suppress to generate the condensation reaction of coke.
Above-mentioned improvement still needs recycle hydrogen and circulating hydrogen compressor, CN200810141293.X has proposed a kind of two-phase hydrogenation method, recycle hydrogen and circulating hydrogen compressor have been cancelled, hydrogen is mixed the formation mixture flow with fresh feed oil and part turning oil in the presence of solvent or thinner, mixture flow in separating tank with after the gas delivery, liquid phase enters reactor and contacts with catalyzer and react, a reaction effluent part is as turning oil, another part degass and obtains product after liquid/gas separator separates, but the inner member of liquid phase hydrogenation reactor is not mentioned as yet, and the liquid phase hydrogenation reactor inner member is the core of reactor, determining the mass transfer and the speed of response of hydrogenation reaction, and the efficient of hydrogenation.
Summary of the invention
The purpose of this utility model is to provide a kind of liquid phase hydrogenation reactor, reactor comprises reactor shell and beds, reactor outlet, reactor inlet and turning oil inlet, with the catalyst bed interlayer mixing tank is set in the reactor head end socket, be provided with the internal recycle oil pipe in the reactor, internal recycle oil pipe one end links to each other with mixing tank feed entrance in the end socket, the internal recycle oil pipe the other end stretches out from reactor bottom, as the turning oil inlet, the dissolved hydrogen that relies on turning oil to carry provides hydrogenation reaction required hydrogen partial for fresh feed.
A kind of liquid phase hydrogenation reactor of the utility model is provided with mixing tank in the reactor head end socket, and mixing tank has mixing oil opening for feed and hydrogen inlet, molten hydrogen mixture outlet and pneumatic outlet, and the molten hydrogen mixture outlet of mixing tank is inserted in the reactor liquid phase.This mixing tank can increase the alternate contact surface of gas-liquid effectively, and is simple in structure, and hydrogen is dissolved in the mixing oil, promotes reaction, improves the efficient of hydrogenation greatly.
Described a kind of liquid phase hydrogenation reactor inlet is arranged on reactor top, particularly top or upper side, and reactor outlet is arranged on reactor lower part, particularly in the bottom or lower side.
Described a kind of liquid phase hydrogenation reactor, reactor head is provided with gas discharge outlet.
Described a kind of liquid phase hydrogenation reactor is provided with mixing tank in the reactor head end socket, and fresh feed, turning oil, hydrogen mix in mixing tank.
Described a kind of liquid phase hydrogenation reactor, mixing tank has mixing oil opening for feed, hydrogen inlet and pneumatic outlet, and the molten hydrogen mixture outlet of mixing tank is immersed in the reactor liquid phase.
A kind of liquid phase hydrogenation reactor described in the utility model removes a kind of pollutent in its sulphur, nitrogen, oxygen, the metallic impurity at least, and saturated aromatic hydrocarbons, changes the hydrocarbon ils molecular structure.
Catalyzer can be single bed or the filling of many beds in a kind of liquid phase hydrogenation reactor described in the utility model, the reactor head end socket is provided with mixing tank, make fresh feed, turning oil and hydrogen mixed dissolution, behind the discharge section gas, molten hydrogen mixture enters beds and contacts with catalyzer and react, concerning many bed reactors, also be provided with mixing tank between bed, the effluent that comes out from first section beds enters the bed mixing tank makes the hydrogen dissolving of injecting between bed wherein, behind the discharge section gas, liquid enters second section beds, contact with catalyzer and to proceed reaction, the rest may be inferred, and reaction effluent is drawn from reactor outlet, and the partial reaction effluent turns back to the reactor head mixing tank as turning oil by the internal recycle oil pipe to be mixed with fresh feed.
The fresh feed oil of a kind of liquid phase hydrogenation reactor described in the utility model is hydrocarbon ils or hydrocarbon ils distillate, as petroleum fractions, distillate, diesel oil, deasphalted oil, residual oil, lubricating oil, liquefied coal coil and shale oil or its product.
A kind of liquid phase hydrogenation reactor of the utility model utilizes mixing tank to make hydrogen be dissolved in that the hydrogenation reaction for hydrocarbon ils provides hydrogen source in the mixing raw material oil.
A kind of liquid phase hydrogenation reactor of the utility model can be used for straight run oil, FCC turning oil, coker gas oil CGO, perhaps it mixes kerosene and diesel oil hydrogenation processing, also can be used for the FCC raw materials pretreatment, be used for new device and relax the hydrocracking transformation, be used to produce ULSD, be used for the aftertreatment of raw materials pretreatment or product.
The utility model liquid phase hydrogenation reactor has following advantage:
1) catalyst levels is few;
2) hydrogen loss is less;
3) lower process cost;
4) liquid yield is higher;
5) bigger flexibility of operation;
6) the sulphur nitrogen content of product is very low;
7) lower investment;
8) reduced reactor volume;
9) for producing ultra-low-sulphur diesel, improvement expenses is very low.
Compare the present invention with the prior art of trickle bed hydrogenator: but desulfurization 90%～98%, and the hydrogen consumption only is 70%～90% of a trickle bed hydrogenator, the total consumption of catalyzer only is 15%～30%.
Description of drawings
Fig. 1, Fig. 2 are respectively a kind of liquid phase hydrogenation reactor of the utility model.
Among the figure: 1. reactor inlet, 2. reactor shell, 3. mixing oil opening for feed, 4. mixing tank, 5. reactor top pneumatic outlet, 6. mixing tank pneumatic outlet, 7. mixing tank hydrogen inlet, 8. beds, 9. internal recycle oil pipe, 10. the molten hydrogen mixture outlet of mixing tank, 11. reactor outlets, 12. turning oils inlet, 13. fresh feed oil, 14. mixing tank gases, 15. hydrogen, 16. reaction effluent, 17. turning oils
Embodiment
Be illustrated in figure 1 as first kind of embodiment of the present invention, reactor shown in the figure is a two-stage catalytic agent bed.By reactor shell 2, reactor inlet 1, mixing tank 4, reactor top pneumatic outlet 5, beds 8, reactor outlet 11 and turning oil inlet 12 are formed, and mixing tank 4 is provided with mixing oil opening for feed 3 and hydrogen inlet 7, the outlet 10 of molten hydrogen mixture and mixing tank pneumatic outlet 6.
Be illustrated in figure 2 as second kind of embodiment of the present invention, reactor shown in the figure is a two-stage catalytic agent bed.By reactor shell 2, reactor inlet 1, mixing tank 4, reactor top pneumatic outlet 5, beds 8, reactor outlet 11 and turning oil inlet 12 are formed, and mixing tank 4 is provided with mixing oil opening for feed 3 and hydrogen inlet 7, the outlet 10 of molten hydrogen mixture and mixing tank pneumatic outlet 6.
Fresh feed oil enters reactor from reactor inlet 1, with enter mixing tank 4 after turning oil 17 mixes, in mixing tank with behind hydrogen 15 thorough mixing that inject, form mixture flow, gas 14 is discharged from mixing tank pneumatic outlet 6 and reactor head pneumatic outlet 5, liquid enters first section beds of reactor and catalyzer contact reacts by the molten hydrogen mixture outlet 10 of mixing tank, the reactant flow of coming out from first section catalyst bed interlayer, enter mixing tank between bed from the mixing tank feed entrance, mix with turning oil 17, hydrogen enters mixing tank from the mixing tank hydrogen inlet, after hydrogen dissolves, molten hydrogen mixture enters second section beds liquid phase from the molten hydrogen mixture outlet of mixing tank outflow and proceeds reaction, gas is discharged from the mixing tank pneumatic outlet, the reaction effluent 16 that comes out from second section beds is through reactor outlet 11 outflow reactors, the partial reaction effluent turns back between reactor head mixing tank and bed by internal recycle oil pipe 9 as turning oil 17 and mixes with reactant flow in the mixing tank, and another part separates and obtains product.
Claims (5)
1. liquid phase hydrogenation reactor, reactor comprises reactor shell (2) and beds (8), reactor outlet (11), reactor inlet (1) and turning oil inlet (12), with the catalyst bed interlayer mixing tank (4) is set in the reactor head end socket, it is characterized in that: be provided with internal recycle oil pipe (9) in the reactor, internal recycle oil pipe one end links to each other with mixing tank opening for feed (3) in the end socket, and the internal recycle oil pipe the other end stretches out from reactor bottom, as turning oil inlet (12).
2. a kind of liquid phase hydrogenation reactor according to claim 1, it is characterized in that: described mixing tank (4) has mixing oil opening for feed (3), mixing tank hydrogen inlet (7), gas mixture gas outlet (6) and the molten hydrogen mixture outlet of mixing tank (10), and the molten hydrogen mixture outlet of mixing tank is immersed in the reactor liquid phase.
3. a kind of liquid phase hydrogenation reactor according to claim 1 is characterized in that: catalyzer in the described liquid phase hydrogenation reactor (8) is single bed or the filling of many beds.
4. a kind of liquid phase hydrogenation reactor according to claim 1 is characterized in that: described internal recycle oil pipe (9) links to each other with the mixing tank opening for feed (3) of catalyst bed interlayer mixing tank (4).
5. a kind of liquid phase hydrogenation reactor according to claim 1 is characterized in that: described reactor head is provided with gas discharge outlet (5).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011201040690U CN202063881U (en) | 2011-04-12 | 2011-04-12 | Liquid-phase hydrogenation reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011201040690U CN202063881U (en) | 2011-04-12 | 2011-04-12 | Liquid-phase hydrogenation reactor |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN202063881U true CN202063881U (en) | 2011-12-07 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2011201040690U Expired - Lifetime CN202063881U (en) | 2011-04-12 | 2011-04-12 | Liquid-phase hydrogenation reactor |
Country Status (1)
| Country | Link |
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| CN (1) | CN202063881U (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103789005A (en) * | 2012-11-03 | 2014-05-14 | 中国石油化工股份有限公司 | Hydrogen dissolution method in two-phase hydrogenation reactor |
| CN111534329A (en) * | 2020-05-25 | 2020-08-14 | 盘锦浩业化工有限公司 | Gasoline hydrogenation and olefin removal treatment method and device |
| WO2021078186A1 (en) | 2019-10-25 | 2021-04-29 | 中国石油化工股份有限公司 | Liquid phase reactor and application thereof |
-
2011
- 2011-04-12 CN CN2011201040690U patent/CN202063881U/en not_active Expired - Lifetime
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103789005A (en) * | 2012-11-03 | 2014-05-14 | 中国石油化工股份有限公司 | Hydrogen dissolution method in two-phase hydrogenation reactor |
| CN103789005B (en) * | 2012-11-03 | 2016-03-02 | 中国石油化工股份有限公司 | Molten hydrogen methods in a kind of two-phase hydrogenation reactor |
| WO2021078186A1 (en) | 2019-10-25 | 2021-04-29 | 中国石油化工股份有限公司 | Liquid phase reactor and application thereof |
| US12037551B2 (en) | 2019-10-25 | 2024-07-16 | China Petroleum & Chemical Corporation | Liquid-phase reactor and application thereof |
| CN111534329A (en) * | 2020-05-25 | 2020-08-14 | 盘锦浩业化工有限公司 | Gasoline hydrogenation and olefin removal treatment method and device |
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Legal Events
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C56 | Change in the name or address of the patentee | ||
| CP01 | Change in the name or title of a patent holder |
Address after: 100728 Beijing, Chaoyangmen, North Street, No. 22, No. Co-patentee after: Luoyang Petrochemical Engineering Corporation /SINOPEC Patentee after: Sinopec Corp. Address before: 100728 Beijing, Chaoyangmen, North Street, No. 22, No. Co-patentee before: Luoyang Petrochemical Engineering Co., China Petrochemical Group Patentee before: Sinopec Corp. |
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| CX01 | Expiry of patent term |
Granted publication date: 20111207 |
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| CX01 | Expiry of patent term |