CN101993719A - Method for hydrogenating hydrocarbon oil and reactor thereof - Google Patents
Method for hydrogenating hydrocarbon oil and reactor thereof Download PDFInfo
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- CN101993719A CN101993719A CN2009100657169A CN200910065716A CN101993719A CN 101993719 A CN101993719 A CN 101993719A CN 2009100657169 A CN2009100657169 A CN 2009100657169A CN 200910065716 A CN200910065716 A CN 200910065716A CN 101993719 A CN101993719 A CN 101993719A
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Abstract
The invention discloses a method for hydrogenating hydrocarbon oil, which is characterized by comprising the following steps of: enabling reactive feed of hydrogen, fresh raw oil and recycle oil to enter a mixer inside a reactor to form mixture flow; enabling the mixture flow to contact a catalyst, wherein part of reaction effluent is used as the recycle oil; immersing a catalyst bed layer in a liquid-phase material, wherein the content of hydrogen in the mixture flow is 1-30 times as much as the saturated hydrogen dissolving capacity of the mixture flow under reaction condition; placing a mixer of hydrocarbon oil and hydrogen in the reactor to reduce the difference of pressure inside and outside the mixer and decrease the wall thickness of the mixer, thereby reducing equipment investment.
Description
Technical field
The present invention relates to the refining hydrocarbon ils of hydrogen, particularly a kind of hydrocarbon oil hydrogenation is made with extra care hydrocarbon ils.
Background technology
In the hydrocarbon ils processing technology, 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, therefore the circulating hydrogen compressor becomes imperative equipment in existing hydrogen addition technology, be called the heart of hydrogenation unit in the industry, this shows its importance in hydrogenation unit.
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 reduce the burden of circulating hydrogen compressor, people begin to consider to utilize hydrogen supply agent to provide hydrogen source for the hydrocarbon oil hydrogenation process, USP4698147 promptly 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, US6428686 has proposed a kind of two-phase hydrogenation method, before reactor, be dissolved in hydrogen in the stock oil, recycle hydrogen and circulating hydrogen compressor have been cancelled, the investment and the process cost of hydrogenation unit have been reduced, this technology adopts the liquid phase circulation of reaction product, improve the meltage of hydrogen, to satisfy in the hydrogenation process requirement to hydrogen, and take reaction heat out of, this technology is with turning oil, enter hydrogenator after raw material and solvent or thinner and hydric solvent or the mixing diluents, advantage is to have reduced the investment and the process cost of circulating hydrogen compressor, its shortcoming is the speed of response that the existence of a large amount of turning oil can influence fresh feed and hydrogen, because fresh feed is relatively fiercer with hydrogen reaction when beginning contacts with catalyzer, turning oil is through hydrogenation reaction, its reactive behavior is lower than fresh feed, therefore the existence of turning oil has hindered contacting of fresh feed oil and hydrogen and catalyzer, has reduced the mass transfer and the speed of response of the oily and hydrogen of fresh feed.
Be recycled directly to the problem that speed of response that reactor inlet brings descends in order to overcome US6428686 turning oil, Chinese patent application CN200810049938.7 has proposed turning oil is entered reactor between the beds, reaction on catalyzer provides fresh hydrogen source for stock oil and hydrogen, and turning oil is from high-pressure separator.As everyone knows, hydrogenation reaction is thermopositive reaction, and the temperature of reactor outlet logistics is higher than reactor inlet temperature.Usually the reactor outlet logistics at first with cold logistics heat exchange, enter high-pressure separator then and carry out gas-liquid separation, it is the separator of a high pressure low temperature that high-pressure separator is compared with reactor, contain hydrogen sulfide from the turning oil that high-pressure separator is told, these hydrogen sulfide can influence the speed of hydrogenating desulfurization and other hydrogenation reactions from entering reactor between reactor inlet or the bed.
Be that US6428686 or CN200810049938.7 are recycled directly to the reactor outlet logistics between reactor inlet or the beds, though CN200810049938.7 is that the liquid phase of will come out from separator is as turning oil, from the liquid phase that separator comes out, contain dissolved hydrogen sulfide, these hydrogen sulfide are in the hydrogenation process, deviate from that sulfide in the raw material produces, this is the hydrogenation reaction desired response, but these hydrogen sulfide in the turning oil can influence activity of such catalysts, suppress sulfocompound near the activity of such catalysts center, reduce activity of such catalysts and selectivity, this is a unwanted results.
US6428686 still is that CN200810049938.7 is arranged at stock oil, turning oil and solvent or thinner outside the reactor with the mixing tank that mixes molten hydrogen of hydrogen, such mixing tank need bear mixing tank inner high voltage medium and the outer atmospheric pressure difference of mixing tank, need thicker wall thickness to bear this pressure difference, such facility investment is higher.
Summary of the invention
The present invention proposes a kind of hydrogenation method for hydrocarbon oils, this method is inserted the mixing tank of hydrocarbon ils and hydrogen in the reactor, reduces the inside and outside pressure difference of mixing tank, reduces its wall thickness and reduces facility investment.
A kind of hydrogenation method for hydrocarbon oils that the present invention removes, be characterised in that: the reaction feed that comprises hydrogen, stock oil and turning oil enters mixing tank in the reactor and forms mixture flow and contact with catalyzer, the reaction effluent part is as turning oil, beds is immersed in the liquid phase material, amounts of hydrogen is 1～30 times of the saturated molten hydrogen amount of mixture flow under reaction conditions in the mixture flow, preferred 1.2～20 times, be preferably 1.5～10 times.
A kind of hydrogenation method for hydrocarbon oils that the present invention removes is characterised in that: reaction feed also comprises solvent or thinner.
Described reaction effluent part is deviate from hydrogen sulfide as turning oil through stripping.
Contain 0.1～15 volume % gas in the described reactor, long-pending in overall reactor.
It is rare gas element or hydrogen that described stripping is deviate from turning oil hydrogen sulfide medium, is preferably hot high pressure hydrogen.
Described reaction feed enters reactor from reactor top, and reaction effluent flows out from reactor lower part.
Described reaction feed enters reactor from reactor lower part, and reaction effluent flows out from reactor top.
Described solvent or thinner are at least a in the hydrocarbon ils behind heavy naphtha, petroleum naphtha, lighter hydrocarbons, benzoline, diesel oil, VGO and the hydrogenation.
Described fresh feed oil is the cut of hydrocarbon ils or hydrocarbon ils, at least a in petroleum fractions, distillate, diesel oil, deasphalted oil, residual oil, lubricating oil, liquefied coal coil and shale oil or its product.
Described hydrogenation method for hydrocarbon oils removes a kind of pollutent in hydrocarbon ils sulphur, nitrogen, oxygen, the metallic impurity at least, saturated aromatic hydrocarbons, and the molecular structure of change hydrocarbon ils.
Described hydrogenation method for hydrocarbon oils utilization enters the pressure of the hydrogen richness controlling reactor in the mixture.
Described hydrogenation method for hydrocarbon oils utilizes the liquid level in the reactor outlet valve controlling reactor.
The volume ratio of described hydrogenation method for hydrocarbon oils turning oil and fresh feed oil is 0.1: 1～20: 1, is preferably 0.5: 1～15: 1.
Described a kind of hydrogenation method for hydrocarbon oils is characterised in that: the mixing tank that hydrogen, solvent or thinner, fresh feed oil and turning oil enter in the reactor forms mixture flow discharge gas, and liquid (molten hydrogen mixture) contacts with catalyzer.
Described a kind of hydrogenation method for hydrocarbon oils is characterised in that: catalyzer is Hydrobon catalyst, catalyst for hydro-upgrading, hydrotreating catalyst or hydrocracking catalyst.
Described a kind of hydrogenation method for hydrocarbon oils is characterised in that: liquid phase material by the reaction conditions of hydrogenation catalyst bed is: temperature of reaction is 150～450 ℃, and reaction pressure is 1～17MPa, and volume space velocity is 0.5～15h during liquid
-1
The invention provides a kind of hydrocarbon oil hydrogenation reactor, comprise reactor shell and beds, reactor outlet and reactor inlet pipe connecting, be characterised in that: the reactor feedstocks inlet is provided with mixing tank, the mixing tank feed entrance that responds, mixing tank also has molten hydrogen mixture and pneumatic outlet, and mixer entrance reactor reaction device inlet links to each other, and mixer outlet links to each other with beds.
Described a kind of hydrocarbon oil hydrogenation reactor, be characterised in that: reactor outlet links to each other with outlet valve.
Reactor inlet is arranged on reactor top, and reactor outlet is arranged on reactor lower part.
Reactor inlet is arranged on reactor lower part, and reactor outlet is arranged on reactor top.
The problem of a maximum of hydrogenation process is the beds coking, the coking reaction can take place under the reaction conditions, if there is not enough hydrogen, the cracking reaction meeting causes coke to form, and is deposited on catalyst surface, and the present invention is owing to adopt the turning oil circulation, it is saturated that turning oil obtains many aromatic hydrocarbons through hydrogenation, function with hydrogen supply can suppress coke and form, and prolongs life of catalyst.
Reaction effluent in a kind of hydrogenation method for hydrocarbon oils of the present invention and the another kind of hydrogenation method for hydrocarbon oils is partly deviate from behind the hydrogen sulfide as turning oil, because of turning oil has been deviate from hydrogen sulfide wherein, so can reduce the harm to catalyzer.
A kind of hydrogenation method for hydrocarbon oils of the present invention and another kind of hydrogenation method for hydrocarbon oils can be used for straight run, 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 pre-treatment of raw material or the aftertreatment of product.
Hydrogenation method for hydrocarbon oils of the present invention 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.
10) reduce catalyzer harm, the life cycle that prolongs catalyzer.
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 is a kind of hydrocarbon oil hydrogenation reactor of the present invention
Fig. 2 is the another kind of hydrocarbon oil hydrogenation reactor of the present invention
Wherein: 1. reaction feed, 2. pneumatic outlet, 3. mixing tank, 4. beds, 5. reactor shell, 6. reactor outlet, 7. outlet valve, 8. molten hydrogen mixture, 9. reactor inlet, 10. reaction effluent, 11 mixer entrances, 12. molten hydrogen mixture outlets, 13. pipe connectings, 14. gases.
Embodiment
Further specify the typical process flow of the inventive method below in conjunction with accompanying drawing, but the inventive method is not limited to concrete mode shown in the drawings.
As shown in Figure 1, Fig. 1 is the reactor of a beds, and reactor inlet 9 is arranged on reactor head.Reactor shown in Figure 1 comprises reactor shell 5, beds 4 and mixing tank 3, mixing tank 3 is arranged on reactor inlet 9 belows, mixing tank is provided with mixer entrance 11, also has molten hydrogen mixture outlet 12 and pneumatic outlet 2, reactor inlet 9 is arranged on the top of reactor shell 1, link to each other with mixer entrance 11 by pipe connecting 13, molten hydrogen mixture outlet 12 links to each other with beds 4, and pneumatic outlet 2 extends to reactor shell 1 outside; Reactor outlet 6 links to each other with outlet valve 7 by pipe connecting 13, and reactor outlet 6 is arranged on reactor shell 1 bottom.
Comprise hydrogen, fresh feed oil and turning oil or hydrogen, fresh feed oil, the reaction feed 1 of solvent or thinner and turning oil forms mixture flow from the mixing tank 3 that reactor inlet 9 enters in the reactor shell 5, discharge gas 2, molten hydrogen mixture 8 enters catalyzer and goes out bed 4 and contact with catalyzer, temperature of reaction is 150～450 ℃, reaction pressure is 1～17MPa, volume space velocity is to carry out hydrogenation under 0.5～15h-1 condition to take off impurity and the saturated aromatic hydrocarbons of hydrogenation during liquid, change the hydrogenation reaction of the molecular structure of hydrocarbon ils, remove sulphur, nitrogen, oxygen, a kind of pollutent in the metallic impurity, saturated aromatic hydrocarbons, change the molecular structure of hydrocarbon ils, reaction effluent 10 is through reactor outlet 6, pipe connecting and outlet valve 7 flow out, reaction effluent 10 parts are as turning oil, part goes out device as product, and beds is immersed in the liquid phase material, and amounts of hydrogen is 1～30 times of the saturated molten hydrogen amount of mixture flow under reaction conditions in the mixture flow, preferred 1.2～20 times, be preferably 1.5～10 times.
As shown in Figure 2, Fig. 2 is the reactor of a beds, and reactor inlet 9 is arranged on reactor bottom.Reactor shown in Figure 1 comprises reactor shell 5, beds 4 and mixing tank 3, mixing tank 3 is arranged on reactor inlet 9 tops, mixing tank is provided with mixer entrance 11, also has molten hydrogen mixture outlet 12 and pneumatic outlet 2, reactor inlet 9 is arranged on the top of reactor shell 1 and links to each other with mixer entrance 11 by pipe connecting 13, molten hydrogen mixture outlet 12 links to each other with beds 4, and pneumatic outlet 2 extends to reactor shell 1 outside; Reactor outlet 6 links to each other with outlet valve 7 by pipe connecting 13, and reactor outlet 6 is arranged on reactor shell 1 top.
Comprise that hydrogen, fresh feed oil and turning oil or hydrogen, fresh feed oil, solvent or thinner and turning oil reaction feed 1 form mixture flow from the mixing tank 3 that reactor inlet 9 enters in the reactor shell 5, discharge gas 2, molten hydrogen mixture 8 enters catalyzer and goes out bed 4 and contact with catalyzer, temperature of reaction is 150～450 ℃, reaction pressure is 1～17MPa, and volume space velocity is 0.5～15h during liquid
-1Carry out hydrogenation under the condition and take off impurity and the saturated aromatic hydrocarbons of hydrogenation, change the hydrogenation reaction of the molecular structure of hydrocarbon ils, remove a kind of pollutent in sulphur, nitrogen, oxygen, the metallic impurity, saturated aromatic hydrocarbons, change the molecular structure of hydrocarbon ils, reaction effluent 10 flows out through reactor outlet 6, pipe connecting and outlet valve 7, reaction effluent 10 parts are as turning oil, part goes out device as product, beds is immersed in the liquid phase material, amounts of hydrogen is 1～30 times of the saturated molten hydrogen amount of mixture flow under reaction conditions in the mixture flow, preferred 1.2～20 times, is preferably 1.5～10 times.
In the inventive method, technology contents such as concrete hydrogenation technique condition and selection of catalysts can be determined according to the conventional knowledge in this area according to feedstock property and quality product requirement.The dissolved hydrogen amount can measuring under the reaction conditions, can calculate according to the experimental formula that this area document provides, can estimate that also above-mentioned experimental formula and empirical value can be with reference to " hydroprocessing technique and engineering " book associated visceras of Sinopec press publication in 2004 according to the empirical value that this area document provides.Determination of test method reactive system dissolved hydrogen amount is a technological method well known to those skilled in the art, as on testing apparatus, adopts the condition identical with reaction process, measures system dissolves hydrogen amount when reaching suitable reaction result.
In the inventive method, the partial hydrogenation product mixes with reaction raw materials as circulation is excellent, with the quiet run of assurance hydrogenation reaction and the work-ing life of catalyzer, internal circulating load can be determined according to the particular case of reactive system, suitably add big cycle volume when for example exothermic heat of reaction is big, reactive chemistry hydrogen consumes and suitably adds big cycle volume etc. when high, and in general internal circulating load is favourable to reaction process greatly, but can cause unfavorable results such as power consumption increase, comprehensively various factors is finally determined.The hydrogenation products that recycles can directly recycle, and also can use through recirculation after the fractionating system.
In the inventive method, the raw material that the hydrogenation technique process is used can comprise gasoline, kerosene, diesel oil, VGO (vacuum distillate), CGO (wax tailings), LCO (catalytic cracking light cycle oil), residual oil, deasphalted oil, lubricated wet goods.According to the requirement of purpose product, hydrogenation technique can comprise hydrofining, hydrotreatment, hydro-upgrading, hydrocracking etc.
In the inventive method, other hydrogenation conditions can determine that by this area general knowledge in general, temperature of reaction is 150～450 ℃ according to raw material properties, quality product requirement etc., and reaction pressure is 1～17MPa, and volume space velocity is 0.5～15h during liquid
-1
In the hydrogenation process of the present invention, hydrogen gas circulating system is not set, the dissolved hydrogen of reactive system provides fresh feed to carry out the needed hydrogen of hydrogenation reaction to rely on a large amount of circulation times of liquid-phase product to carry into, because recycling of hydrogenation products still can keep activity of such catalysts stability.Reactor adopts close structural response device with trickle-bed reactor, comes amount of liquid and pressure in the controlling reactor by controlling reactor free air delivery and lifting rate.Its advantage is to eliminate H in the wetting factor influence of catalyzer and the recycle hydrogen
2S and NH
3Influence; Because the specific heat capacity of turning oil is big, thereby reduce the temperature rise of reactor greatly, improve the utilising efficiency of catalyzer, and can reduce side reaction such as cracking, simultaneously can the required amounts of hydrogen of protective reaction.One of characteristics of the present invention are to require to determine to sneak into amounts of hydrogen in the charging according to reaction, come amount of liquid and pressure in the controlling reactor by controlling reactor free air delivery and lifting rate.
Claims (25)
1. hydrogenation method for hydrocarbon oils, it is characterized in that: the reaction feed that comprises hydrogen, stock oil and turning oil enters the interior mixing tank formation mixture flow of reactor, mixture flow contacts with catalyzer, beds is immersed in the liquid phase material, the reaction effluent part is as turning oil, part is as product, and amounts of hydrogen is 1～30 times of the saturated molten hydrogen amount of mixture flow under reaction conditions in the mixture flow.
2. according to the described method of claim 1, it is characterized in that: reaction feed also comprises solvent or thinner.
3. according to claim 1 or 2 described methods, it is characterized in that: the partial reaction effluent is deviate from hydrogen sulfide as turning oil through stripping.
4. according to claim 1 or 2 described methods, it is characterized in that: contain 0.1～15 volume % gas in the reactor, and long-pending in overall reactor.
5. according to the described method of claim 3, it is characterized in that: described stripping medium is rare gas element or hydrogen.
6. according to the described method of claim 3, it is characterized in that: described stripping medium is a hot high pressure hydrogen.
7. according to claim 1 or 2 described methods, it is characterized in that: amounts of hydrogen is 1.2～20 times of the saturated molten hydrogen amount of mixture flow under reaction conditions in the mixture flow.
8. according to claim 1 or 7 described hydrogen methods, it is characterized in that: amounts of hydrogen is 1.5～10 times of the saturated molten hydrogen amount of mixture flow under reaction conditions in the mixture flow.
9. according to the described method of claim 2, it is characterized in that: solvent or thinner are at least a in the hydrocarbon ils behind heavy naphtha, petroleum naphtha, lighter hydrocarbons, benzoline, diesel oil, VGO and the hydrogenation.
10. according to claim 1 or 2 described methods, it is characterized in that: stock oil is at least a in fraction oil of petroleum, atmospheric distillate, vacuum distillate diesel oil, deasphalted oil, residual oil, lubricating oil, liquefied coal coil and shale oil or its product.
11., it is characterized in that: utilize to enter the pressure of the hydrogen richness controlling reactor in the mixture according to claim 1 or 2 described methods.
12., it is characterized in that: utilize the liquid phase liquid level in the reactor outlet valve controlling reactor according to claim 1 or 2 described methods.
13. according to claim 1 or 2 described methods, it is characterized in that: the volume ratio of turning oil and stock oil is 0.1～20: 1.
14. according to the described method of claim 13, it is characterized in that: the volume ratio of turning oil and fresh feed oil is 05～15: 1.
15. according to claim 1 or 2 described methods, it is characterized in that: the mixing tank that hydrogen, solvent or thinner, stock oil and turning oil enter in the reactor forms mixture flow, and mixture flow is discharged gas, and liquid contacts with catalyzer.
16. according to claim 1 or 2 described methods, it is characterized in that: catalyzer is Hydrobon catalyst, catalyst for hydro-upgrading, hydrotreating catalyst or hydrocracking catalyst.
17. according to claim 1 or 2 described methods, it is characterized in that: material by the reaction conditions of hydrogenation catalyst bed is: temperature of reaction is 150～450 ℃, and reaction pressure is 1～17MPa, volume space velocity is 0.5～15h during liquid
-1
18. according to the described method of claim 1, it is characterized in that: the mixing tank that reaction feed enters in the reactor forms mixture flow, gets rid of gas, and liquid contacts with catalyzer.
19. according to the described method of claim 1, it is characterized in that: reaction feed enters reactor from reactor top, and reaction effluent flows out from reactor lower part.
20. according to the described method of claim 1, it is characterized in that: reaction feed enters reactor from reactor lower part, reaction effluent flows out from reactor top.
21. a hydrocarbon oil hydrogenation reactor comprises reactor shell and beds, reactor inlet and reactor outlet is characterized in that: mixing tank is set in the reactor, and the mixing tank feed entrance that responds also has the mixture outlet and the pneumatic outlet of molten hydrogen.
22. according to the described reactor of claim 21, mixing tank reaction feed inlet links to each other with reactor inlet, the mixture outlet of molten hydrogen links to each other with beds, and pneumatic outlet extends to the reactor outside.
23. according to the described reactor of claim 21, it is characterized in that: reactor outlet links to each other with outlet valve.
24. according to the described reactor of claim 21, it is characterized in that: reactor inlet is arranged on reactor top, and reactor outlet is arranged on reactor lower part.
25. according to the described reactor of claim 21, it is characterized in that: reactor inlet is arranged on reactor lower part, reactor outlet is arranged on reactor top.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
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| WO2014044195A1 (en) * | 2012-09-21 | 2014-03-27 | 中国石油化工股份有限公司 | Reformate hydrotreatment method |
| US9862896B2 (en) | 2012-09-21 | 2018-01-09 | China Petroleum & Chemical Corporation | Hydrocarbon oil hydrotreating method |
| 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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| US20050082202A1 (en) * | 1997-06-24 | 2005-04-21 | Process Dynamics, Inc. | Two phase hydroprocessing |
| CN101194001A (en) * | 2005-03-24 | 2008-06-04 | 过程动力学公司 | Control system method and apparatus for continuous liquid phase hydroprocessing |
| CN101280217A (en) * | 2008-06-02 | 2008-10-08 | 中国石油化工集团公司 | Liquid-solid two-phase hydrogenation method for hydrocarbon oil |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| US20050082202A1 (en) * | 1997-06-24 | 2005-04-21 | Process Dynamics, Inc. | Two phase hydroprocessing |
| CN101194001A (en) * | 2005-03-24 | 2008-06-04 | 过程动力学公司 | Control system method and apparatus for continuous liquid phase hydroprocessing |
| CN101280217A (en) * | 2008-06-02 | 2008-10-08 | 中国石油化工集团公司 | Liquid-solid two-phase hydrogenation method for hydrocarbon oil |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2014044195A1 (en) * | 2012-09-21 | 2014-03-27 | 中国石油化工股份有限公司 | Reformate hydrotreatment method |
| RU2609780C2 (en) * | 2012-09-21 | 2017-02-03 | Чайна Петролиум Энд Кемикл Корпорейшн | Reformate hydrotreatment method and apparatus |
| 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 |
| 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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Address after: 100728 Beijing, Chaoyangmen, North Street, No. 22, No. Applicant after: China Petrochemical Group Corp. Co-applicant after: Luoyang Petrochemical Engineering Corporation /SINOPEC Address before: 100728 Beijing, Chaoyangmen, North Street, No. 22, No. Applicant before: China Petrochemical Group Corp. Co-applicant before: Luoyang Petrochemical Engineering Co., China Petrochemical Group |
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| C12 | Rejection of a patent application after its publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20110330 |