CN201644076U - Liquid-phase hydrogenated reactor - Google Patents
Liquid-phase hydrogenated reactor Download PDFInfo
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- CN201644076U CN201644076U CN2010201565374U CN201020156537U CN201644076U CN 201644076 U CN201644076 U CN 201644076U CN 2010201565374 U CN2010201565374 U CN 2010201565374U CN 201020156537 U CN201020156537 U CN 201020156537U CN 201644076 U CN201644076 U CN 201644076U
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Abstract
The utility model discloses a liquid-phase hydrogenated reactor, which comprises a reactor barrel body, catalyst beds, a reactor outlet and a reactor inlet. The liquid-phase hydrogenated reactor is characterized in that mixers are disposed among the catalyst beds, each mixer is provided with a feed inlet and a hydrogen inlet, a hydrogen dissolving mixture outlet and a gas outlet, the hydrogen dissolving mixture outlet of each mixer is immersed in liquid of a next catalyst bed, and the mixers can effectively increase contact area between gas and liquid, are simple in structure, lead hydrogen to be dissolved in mixing oil, promote reaction, and greatly increase hydrogenation efficiency.
Description
Technical field
The present invention relates to hydrogen and have hydrocarbon oil refining field down, particularly a kind of liquid phase hydrogenation reactor.
Background technology
The sustainable development of World Economics 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 product quality that these two kinds of technologies obtain generally is difficult to the quality index requirement that reaches strict.In the light Fuel product quality system, sulfur content is most important index, how to reduce sulfur content in the oil product and be one of most significant problems that current petroleum chemical industry faces, the Cetane number 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 extensive 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, is adsorbed on the surface of catalyst then jointly, reacts under the effect of catalyst active center.Because hydrogenation reaction is a strong exothermal reaction, in order to keep reaction temperature, utilize a large amount of hydrogen and feedstock 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 hydrogenation reactor 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 main cause of excessive hydrogen, keeps higher hydrogen branch and is pressed in and helps hydrofinishing 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 that the effect of circulating hydrogen compressor will not participate in hydrogenation reaction exactly improves pressure recycles it, so the circulating hydrogen compressor becomes imperative equipment in existing hydrogen addition technology, is called the heart of hydrogenation plant 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 catalyst.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 feedstock oil is generally 50～2000: 1, therefore the hydrogenation reactor design is bigger, and the actual feedstock oil that reacts of participating in is relevant with liquid hourly space velocity (LHSV), air speed has reflected the disposal ability of device, and bigger air speed operation is adopted in industrial hope, but air speed is subjected to the restriction of reaction speed.Air speed is unusual at 0.5～10h according to catalyst activity, feedstock property, reaction depth
-1Between the fluctuation.The unifining process of commercial Application can improve alkene saturation factor, hydrodesulfurization rate and hydrodenitrogeneration rate at certain reaction temperature condition decline low-speed at present.Under hydrocracking condition, it is little to total conversion ratio influence to improve air speed, but the decline of the light component content in the 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 operating 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 time of staying, 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 formation with fresh feed oil and part recycle oil mix logistics in the presence of solvent or diluent, after mixing logistics and in knockout drum, gas being separated, liquid phase enters reactor and contacts with catalyst and react, a reaction effluent part is as recycle oil, another part degass and obtains product after liquid/gas separator separates, but the inner member of hydrogenation reactor is not mentioned as yet, and the hydrogenation reactor inner member is the core of reactor, determining the mass transfer and the reaction speed of hydrogenation reaction, and the efficient of hydrogenation.
The utility model content
The purpose of this utility model is to provide a kind of liquid phase hydrogenation reactor, and this reactor beds interlayer is provided with the bed blender, and this blender can increase the alternate contact-making surface of gas-liquid effectively, simple in structure, hydrogen is dissolved in the miscella, promotes reaction, improve the efficient of hydrogenation greatly.
A kind of liquid phase hydrogenation reactor of the utility model, reactor comprises reactor shell and beds, reactor outlet and reactor inlet, be characterised in that: blender is set between the beds, blender has charging and hydrogen inlet, blender also has molten hydrogen mixture and gas vent, and the molten hydrogen mixture outlet of blender is inserted in the beds.
Described a kind of liquid phase hydrogenation reactor, one or more sealed liquid outlets are established in the beds that links to each other with blender feed entrance outlet.
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.
Reactor inlet is arranged on reactor lower part, and particularly in the bottom or lower side, reactor outlet is arranged on reactor top, particularly top or upper side.
Described a kind of liquid phase hydrogenation reactor, its feature also is: reactor head is provided with gas discharge outlet.
Described a kind of liquid phase hydrogenation reactor, its feature also is: one or more sealed liquid outlets are established in the reactor bed bottom, link to each other with the blender feed entrance.
Described a kind of liquid phase hydrogenation reactor, its feature also is: the molten hydrogen mixture outlet of blender is immersed in the next beds liquid phase.
A kind of liquid phase hydrogenation reactor described in the utility model removes a kind of pollutant in its sulphur, nitrogen, oxygen, the metal impurities at least, and saturated aromatic hydrocarbons, changes the hydrocarbon ils molecular structure.
Catalyst divides two sections bed fillings at least in a kind of liquid phase hydrogenation reactor described in the utility model, the catalyst bed interlayer is provided with the bed blender, the effluent that the hydrogen that injects between bed is dissolved in come out from first section beds, behind the discharge section gas, liquid enter second bed contact with catalyst proceed the reaction, the effluent that comes out from second section beds enters the bed blender makes the hydrogen dissolving of injecting between bed wherein, behind the discharge section gas, liquid enters the 3rd section beds, contact with catalyst and to proceed reaction, the rest may be inferred, and reaction effluent is drawn from reactor outlet.
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 distillate, 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 the bed blender between bed to make hydrogen be dissolved in that the hydrogenation reaction for hydrocarbon ils provides hydrogen source in the effluent that each section beds comes out.
A kind of liquid phase hydrogenation reactor of the utility model can be used for straight-run oil, FCC recycle oil, coker gas oil CGO, perhaps it mixes kerosene and diesel oil hydrogenation processing, also can be used for the FCC pretreatment of raw material, be used for new device and relax the hydrocracking transformation, be used to produce ULSD, be used for the post processing of pretreatment of raw material or product.
The utility model liquid phase hydrogenation reactor has following advantage:
1) catalyst amount is few;
2) hydrogen loss is less;
3) lower operating cost;
4) liquid yield is higher;
5) bigger operating flexibility;
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 hydrogenation reactor: but desulfurization 90%～98%, and the hydrogen consumption only is 70%～90% of a trickle bed hydrogenation reactor, the total consumption of catalyst only is 15%～30%.
Description of drawings
Fig. 1 is a kind of liquid phase hydrogenation reactor of the utility model.
Among the figure: 1. reactor inlet, 2. reactor shell, 3. blender feed entrance, 4. blender, 5. reactor top gas vent, 6. blender gas vent, 7. blender hydrogen inlet, 8. beds, 9. beds, 10. reactor outlet, 11. mixer outlets, 12. mix logistics, 13. reactor top gas, 14. blender gases, 15. hydrogen, 16. reaction effluent, 17. liquid levels
The specific embodiment
As shown in Figure 1, reactor shown in the figure is a two-stage catalytic agent bed.By reactor shell 2, reactor inlet 1, blender 4, reactor top gas vent 5, beds 8,9 beds and reactor outlet 10 are formed, and blender 4 is provided with feed entrance 3 and hydrogen inlet 7, the outlet 11 of molten hydrogen mixture and blender gas vent 6.
Fresh feed oil mixes formation with hydrogen and recycle oil and mixes logistics in mixing dissolver, mix logistics and enter reactor from reactor inlet 1, discharge reactor top gas 13 from reactor head gas vent 5, liquid enters first section beds of reactor and catalyst haptoreaction, the reactor stream of coming out from the first catalyst bed interlayer, enter blender 4 from feed entrance 3, hydrogen enters blender from hydrogen inlet 7, after hydrogen dissolves, molten hydrogen mixture enters the second beds liquid phase from molten hydrogen mixture outlet 11 outflows and proceeds reaction, gas is discharged from blender gas vent 6, the reaction effluent 16 that comes out from second beds is through reactor outlet 10 outflow reactors, the effluent part partly separates obtaining product as recycle oil.
Claims (9)
1. liquid phase hydrogenation reactor, reactor comprises reactor shell and beds, reactor outlet and reactor inlet, be characterised in that: blender is set between the beds, blender has charging and hydrogen inlet, blender also is provided with molten hydrogen mixture outlet and gas vent, and the molten hydrogen mixture outlet of blender is immersed in next beds liquid.
2. according to the described a kind of liquid phase hydrogenation reactor of claim 1, it is characterized in that: reactor inlet is arranged on reactor top, and reactor outlet is arranged on reactor lower part.
3. according to the described a kind of liquid phase hydrogenation reactor of claim 1, it is characterized in that: reactor inlet is arranged on bottom or lower side, and reactor outlet is provided with top or upper side.
4. according to the described a kind of liquid phase hydrogenation reactor of claim 1, it is characterized in that: reactor inlet is arranged on reactor lower part, and reactor outlet is arranged on reactor top.
5. according to the described a kind of liquid phase hydrogenation reactor of claim 1, it is characterized in that: reactor inlet is arranged on top or upper side, and reactor outlet is provided with bottom or lower side.
6. according to the described a kind of liquid phase hydrogenation reactor of claim 1, it is characterized in that: reactor head is provided with gas discharge outlet.
7. according to the described a kind of liquid phase hydrogenation reactor of claim 1, it is characterized in that: hydrogenation reactor is provided with two beds at least.
8. according to the described a kind of liquid phase hydrogenation reactor of claim 1, it is characterized in that: the beds outlet that links to each other with the blender feed entrance is provided with one or more liquid outlets.
9. according to the described a kind of liquid phase hydrogenation reactor of claim 8, it is characterized in that: the beds outlet that links to each other with the blender feed entrance is provided with one or more sealed liquid outlets.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
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| CN2010201565374U CN201644076U (en) | 2010-04-13 | 2010-04-13 | Liquid-phase hydrogenated reactor |
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| CN2010201565374U CN201644076U (en) | 2010-04-13 | 2010-04-13 | Liquid-phase hydrogenated reactor |
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Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102732299A (en) * | 2011-04-12 | 2012-10-17 | 中国石油化工股份有限公司 | Hydrocarbon oil two-phase hydrogenation method |
| CN103074102A (en) * | 2011-10-25 | 2013-05-01 | 中国石油化工股份有限公司 | Continuous liquid phase hydrotreatment method for hydrocarbon oil |
| CN103666545A (en) * | 2012-09-21 | 2014-03-26 | 中国石油化工股份有限公司 | Diesel oil hydro-refining method |
| CN103666547A (en) * | 2012-09-21 | 2014-03-26 | 中国石油化工股份有限公司 | Hydrocarbon oil hydrogenation treatment method |
| CN103785332A (en) * | 2012-11-03 | 2014-05-14 | 中国石油化工股份有限公司 | A two-phase hydrogenation reactor and applications thereof |
| CN104232154A (en) * | 2013-06-21 | 2014-12-24 | 中国石油天然气股份有限公司 | Distillate oil hydro-upgrading method |
| CN105602619A (en) * | 2015-12-18 | 2016-05-25 | 中国石油天然气股份有限公司 | Liquid-phase hydrogenation heterogeneous system and process and application thereof |
| US9862896B2 (en) | 2012-09-21 | 2018-01-09 | China Petroleum & Chemical Corporation | Hydrocarbon oil hydrotreating method |
| US9879186B2 (en) | 2012-09-21 | 2018-01-30 | China Petroleum & Chemical Corporation | Reformate hydrotreatment method |
| CN109679689A (en) * | 2017-10-19 | 2019-04-26 | 中国石油化工股份有限公司 | A kind of liquid phase hydrogenation reactor and process for selective hydrogenation and reaction system |
| CN111068587A (en) * | 2018-10-22 | 2020-04-28 | 中国石油化工股份有限公司 | Liquid phase hydrogenation reaction device and reaction method |
| CN112705120A (en) * | 2019-10-25 | 2021-04-27 | 中国石油化工股份有限公司 | Heavy oil processing device and processing method |
-
2010
- 2010-04-13 CN CN2010201565374U patent/CN201644076U/en not_active Expired - Lifetime
Cited By (21)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102732299A (en) * | 2011-04-12 | 2012-10-17 | 中国石油化工股份有限公司 | Hydrocarbon oil two-phase hydrogenation method |
| CN103074102A (en) * | 2011-10-25 | 2013-05-01 | 中国石油化工股份有限公司 | Continuous liquid phase hydrotreatment method for hydrocarbon oil |
| CN103074102B (en) * | 2011-10-25 | 2016-03-02 | 中国石油化工股份有限公司 | A kind of Continuous Liquid Phase method for hydrotreating hydrocarbon oil |
| US9862896B2 (en) | 2012-09-21 | 2018-01-09 | China Petroleum & Chemical Corporation | Hydrocarbon oil hydrotreating method |
| CN103666545A (en) * | 2012-09-21 | 2014-03-26 | 中国石油化工股份有限公司 | Diesel oil hydro-refining method |
| CN103666547A (en) * | 2012-09-21 | 2014-03-26 | 中国石油化工股份有限公司 | Hydrocarbon oil hydrogenation treatment method |
| CN103666545B (en) * | 2012-09-21 | 2015-09-23 | 中国石油化工股份有限公司 | A kind of diesel oil hydrofining method |
| CN103666547B (en) * | 2012-09-21 | 2015-09-23 | 中国石油化工股份有限公司 | A kind of method for hydrotreating hydrocarbon oil |
| US9879186B2 (en) | 2012-09-21 | 2018-01-30 | China Petroleum & Chemical Corporation | Reformate hydrotreatment method |
| CN103785332A (en) * | 2012-11-03 | 2014-05-14 | 中国石油化工股份有限公司 | A two-phase hydrogenation reactor and applications thereof |
| CN103785332B (en) * | 2012-11-03 | 2016-04-13 | 中国石油化工股份有限公司 | A kind of two-phase hydrogenation reactor and application |
| CN104232154A (en) * | 2013-06-21 | 2014-12-24 | 中国石油天然气股份有限公司 | Distillate oil hydro-upgrading method |
| CN104232154B (en) * | 2013-06-21 | 2016-04-06 | 中国石油天然气股份有限公司 | A kind of distillate hydrogenation method for modifying |
| CN105602619A (en) * | 2015-12-18 | 2016-05-25 | 中国石油天然气股份有限公司 | Liquid-phase hydrogenation heterogeneous system and process and application thereof |
| US10683459B2 (en) | 2015-12-18 | 2020-06-16 | Petrochina Company Limited | Liquid-phase hydroisomerization system and process therefor and use thereof |
| CN109679689A (en) * | 2017-10-19 | 2019-04-26 | 中国石油化工股份有限公司 | A kind of liquid phase hydrogenation reactor and process for selective hydrogenation and reaction system |
| CN109679689B (en) * | 2017-10-19 | 2021-03-05 | 中国石油化工股份有限公司 | Liquid-phase hydrogenation reactor, hydrogenation reaction method and reaction system |
| CN111068587A (en) * | 2018-10-22 | 2020-04-28 | 中国石油化工股份有限公司 | Liquid phase hydrogenation reaction device and reaction method |
| CN111068587B (en) * | 2018-10-22 | 2021-08-31 | 中国石油化工股份有限公司 | Liquid phase hydrogenation reaction device and reaction method |
| CN112705120A (en) * | 2019-10-25 | 2021-04-27 | 中国石油化工股份有限公司 | Heavy oil processing device and processing method |
| CN112705120B (en) * | 2019-10-25 | 2022-07-08 | 中国石油化工股份有限公司 | Heavy oil processing device and processing method |
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Address after: 100728 Beijing, Chaoyangmen, North Street, No. 22, No. Co-patentee after: Luoyang Petrochemical Engineering Corporation /SINOPEC Patentee after: China Petrochemical Group Corp. Address before: 100728 Beijing, Chaoyangmen, North Street, No. 22, No. Co-patentee before: Luoyang Petrochemical Engineering Co., China Petrochemical Group Patentee before: China Petrochemical Group Corp. |
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Granted publication date: 20101124 |
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