CN101358146A - Hydrocarbon oil hydrogenation technique - Google Patents
Hydrocarbon oil hydrogenation technique Download PDFInfo
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- CN101358146A CN101358146A CNA200810141293XA CN200810141293A CN101358146A CN 101358146 A CN101358146 A CN 101358146A CN A200810141293X A CNA200810141293X A CN A200810141293XA CN 200810141293 A CN200810141293 A CN 200810141293A CN 101358146 A CN101358146 A CN 101358146A
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Abstract
The present invention discloses a hydrocarbon oil-hydrogenating technique. The technique is free from circulating hydrogen and a circulating hydrogen compressor; with solvent or diluting agent, hydrogen is mixed with fresh raw oil and part of circulating oil to form mixed material flow, which enters into a reactor to be contacted with catalyst; another part or all of circulating oil is mixed with hydrogen; one route or branch passes between the catalyst beds of the reactor to enter into the reactor; one part of reaction outflow is used as circulating oil, and the other part is used as the product after the gas and the solvent or the diluting agent are separated out; and the dissolubility of hydrogen in the solvent or the diluting agent is larger than the dissolubility of hydrogen in the mixture of the fresh raw oil and the solvent or the diluting agent.
Description
Technical field
The present invention relates to the hydrocarbon oil hydrogenation technology, particularly liquid-solid two-phase hydrocarbon oil hydrogenation technology.
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, 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 fluctuates between 0.5～10h-1 according to catalyst activity, feedstock property, the unusual of reaction depth.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 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 be with turning oil with enter hydrogenator after stock oil and hydrogen mix, 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, the existence of turning oil has suppressed the touch opportunity of fresh feed oil and hydrogen and catalyzer, has reduced the mass transfer and the speed of response of fresh feed oil and hydrogen.
Summary of the invention
The present invention proposes a kind of hydrocarbon oil hydrogenation technique, cancelled recycle hydrogen and circulating hydrogen compressor, strengthen the touch opportunity of fresh feed oil and hydrogen and catalyzer, improve mass transfer and speed of response, reduced reactor volume.
A kind of hydrocarbon oil hydrogenation technique of the present invention is: hydrogen mixes the formation mixture flow with fresh feed oil and part turning oil in the presence of solvent or thinner, mixture flow enters reactor and contacts with catalyzer, another part or whole turning oil mix with hydrogen, one the tunnel or along separate routes between the reactor catalyst bed, enter reactor, a reaction effluent part is as turning oil, and another part is isolated behind gas and solvent or the thinner as product.Hydrogen in solvent or thinner solubleness greater than the solubleness of hydrogen in fresh feed oil and solvent or diluent mixture.
Described mixture flow enters reactor from reactor top, and reaction effluent flows out from reactor lower part.
Described mixture flow enters reactor from reactor lower part, and reaction effluent flows out from reactor top.
Described another part or whole turning oil mix with hydrogen in the presence of solvent or thinner.
Described reaction effluent is isolated behind the gas part as turning oil, and another part is isolated behind solvent or the thinner as product.
Described mixture flow enters reactor after isolating gas.
Described mixture flow is mixed in mixing tank, and gas is laggard goes into reactor from going out from mixing tank top.
Described a kind of hydrocarbon oil hydrogenation technique, its feature also is: from going out the laggard mixture flow of going into reactor of gas, liquid contacts with catalyzer from mixing tank top, and gas is got rid of from reactor top.
Described a kind of hydrocarbon oil hydrogenation technique, it is characterized in that: from mixing tank top from going out the laggard mixture flow of going into reactor of gas, liquid and catalyzer contact reacts, gas is got rid of from reactor top, another part or after all turning oil mixes eliminating gas with hydrogen, the one tunnel or shunt between the reactor catalyst bed, enter reactor.
Described a kind of hydrocarbon oil hydrogenation technique, its feature also is: hydrogen mixes the formation mixture flow with fresh feed oil and part turning oil.
The present invention proposes another kind of hydrocarbon oil hydrogenation technique, it is characterized in that: fresh feed oil with in the presence of solvent or thinner, mix the formation mixture flow after part turning oil mixes again with hydrogen, mixture flow enters reactor and contacts with catalyzer, another part or whole turning oil mix with hydrogen, one the tunnel or along separate routes between the reactor catalyst bed, enter reactor, a reaction effluent part is as turning oil, and another part is isolated behind gas and solvent or the thinner as product.The solubleness of hydrogen in solvent or thinner is greater than the solubleness of hydrogen in fresh feed oil and solvent or diluent mixture.
Described another kind of hydrocarbon oil hydrogenation technique, its feature also is: mixture flow enters reactor from reactor top, and reaction effluent flows out from reactor lower part.
Described another kind of hydrocarbon oil hydrogenation technique, its feature also is: mixture flow enters reactor from reactor lower part, and reaction effluent flows out from reactor top.
Described reaction effluent is isolated behind the gas part as turning oil, and another part is isolated behind solvent or the thinner as product.
Described another part or whole turning oil mix with hydrogen in the presence of solvent or thinner.
Described another kind of hydrocarbon oil hydrogenation technique, its feature also is: mixture flow enters reactor after isolating gas.
Described another kind of hydrocarbon oil hydrogenation technique, its feature also is: mixture flow is mixed in mixing tank, and gas is laggard goes into reactor from going out from mixing tank top.
Described another kind of hydrocarbon oil hydrogenation technique, its feature also is: from mixing tank top from going out the laggard mixture flow of going into reactor of gas, liquid and catalyzer contact reacts, gas is got rid of from reactor top.
Described a kind of hydrocarbon oil hydrogenation technique, it is characterized in that: from mixing tank top from going out the laggard mixture flow of going into reactor of gas, liquid and catalyzer contact reacts, gas is got rid of from reactor top, another part or after all turning oil mixes eliminating gas with hydrogen, the one tunnel or shunt between the reactor catalyst bed, enter reactor.
Described another kind of hydrocarbon oil hydrogenation technique, its feature also is: hydrogen mixes the formation mixture flow with fresh feed oil and turning oil.
The invention provides another kind of hydrocarbon oil hydrogenation technique, mix with hydrogen after fresh feed oil, part turning oil and solvent or the mixing diluents and form mixture flow, mixture flow enters reactor and contacts with catalyzer, another part or whole turning oil mix with hydrogen, one the tunnel or along separate routes between the reactor catalyst bed, enter reactor, a reaction effluent part is as turning oil, and another part is isolated behind gas and solvent or the thinner as product.The solubleness of hydrogen in solvent or thinner is greater than the solubleness of hydrogen in fresh feed oil and solvent or diluent mixture.
Described mixture flow enters reactor from reactor top, and reaction effluent flows out from reactor lower part.
Described mixture flow enters reactor from reactor lower part, and reaction effluent flows out from reactor top.
Described another part or whole turning oil mix with hydrogen in the presence of solvent or thinner.
Described reaction effluent is isolated behind the gas part as turning oil, and another part is isolated behind solvent or the thinner as product.
Described mixture flow enters reactor after isolating gas.
Described mixture flow is mixed in mixing tank, and gas is laggard goes into reactor from going out from mixing tank top.
Described a kind of hydrocarbon oil hydrogenation technique, its feature also is: from going out the laggard mixture flow of going into reactor of gas, liquid contacts with catalyzer from mixing tank top, and gas is got rid of from reactor top.
Described a kind of hydrocarbon oil hydrogenation technique, it is characterized in that: from mixing tank top from going out the laggard mixture flow of going into reactor of gas, liquid and catalyzer contact reacts, gas is got rid of from reactor top, another part or after all turning oil mixes eliminating gas with hydrogen, the one tunnel or shunt between the reactor catalyst bed, enter reactor.
Described a kind of hydrocarbon oil hydrogenation technique, its feature also is: hydrogen mixes the formation mixture flow with fresh feed oil and part turning oil.
The present invention proposes another kind of hydrocarbon oil hydrogenation technique, it is characterized in that: mix the formation mixture flow again with part turning oil and hydrogen after fresh feed oil and solvent or the mixing diluents, mixture flow enters reactor and contacts with catalyzer, another part or whole turning oil mix with hydrogen, one the tunnel or along separate routes between the reactor catalyst bed, enter reactor, a reaction effluent part is as turning oil, and another part is isolated behind gas and solvent or the thinner as product.The solubleness of hydrogen in solvent or thinner is greater than the solubleness of hydrogen in fresh feed oil and solvent or diluent mixture.
Described mixture flow enters reactor from reactor top, and reaction effluent flows out from reactor lower part.
Described mixture flow enters reactor from reactor lower part, and reaction effluent flows out from reactor top.
Described another part or whole turning oil mix with hydrogen in the presence of solvent or thinner.
Described reaction effluent is isolated behind the gas part as turning oil, and another part is isolated behind solvent or the thinner as product.
Described mixture flow enters reactor after isolating gas.
Described mixture flow is mixed in mixing tank, and gas is laggard goes into reactor from going out from mixing tank top.
Described a kind of hydrocarbon oil hydrogenation technique, its feature also is: from going out the laggard mixture flow of going into reactor of gas, liquid contacts with catalyzer from mixing tank top, and gas is got rid of from reactor top.
Described a kind of hydrocarbon oil hydrogenation technique, it is characterized in that: from mixing tank top from going out the laggard mixture flow of going into reactor of gas, liquid and catalyzer contact reacts, gas is got rid of from reactor top, another part or after all turning oil mixes eliminating gas with hydrogen, the one tunnel or shunt between the reactor catalyst bed, enter reactor.
Described a kind of hydrocarbon oil hydrogenation technique, its feature also is: hydrogen mixes the formation mixture flow with fresh feed oil and part turning oil.
A kind of hydrocarbon oil hydrogenation technique of the present invention and another kind of hydrocarbon oil hydrogenation technique remove a kind of pollutent in its sulphur, nitrogen, oxygen, the metallic impurity at least, and saturated aromatic hydrocarbons, change the molecular structure of hydrocarbon ils.
Catalyzer divides two sections bed fillings at least in the hydrogenator of the present invention, form two-stage catalytic agent bed at least, the effluent that comes out from first section beds and the turning oil of introducing are mixed into second section beds, contact with catalyzer and to proceed reaction, the effluent that comes out from second section beds with enter the 3rd section beds after the turning oil of introducing mixes, the rest may be inferred, and reaction effluent is drawn from reactor lower part.
Solvent of the present invention or thinner are at least a in the hydrocarbon ils behind heavy naphtha, petroleum naphtha, lighter hydrocarbons, benzoline, diesel oil, VGO and the hydrogenation.
The fresh feed oil of a kind of hydrocarbon oil hydrogenation technique of the present invention and another kind of hydrocarbon oil hydrogenation technique is the distillate of hydrocarbon ils or hydrocarbon ils, as petroleum fractions, distillate, diesel oil, deasphalted oil, residual oil, lubricating oil, liquefied coal coil and shale oil or its product.
A kind of hydrocarbon oil hydrogenation technique of the present invention and another kind of hydrocarbon oil hydrogenation technique have been cancelled recycle hydrogen and circulating hydrogen compressor, utilize hydrocarbon ils, solvent or thinner that hydrogen is dissolved in wherein, for hydrocarbon oil hydrogenation provides hydrogen source, wherein solvent or thinner to the dissolving power of hydrogen greater than hydrocarbon ils, the addition of solvent or thinner is according to the amount of the required hydrogen of hydrocarbon oil hydrogenation process reaction, and promptly chemical hydrogen consumes and regulates.
A kind of hydrocarbon oil hydrogenation technique of the present invention and another kind of hydrocarbon oil hydrogenation technique: utilize the ratio of mixture of turning oil and fresh feed oil to control the temperature that mixture flow enters reactor, utilize the circulation oil mass controlling reactor temperature that enters between the beds.
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.
A kind of hydrocarbon oil hydrogenation technique of the present invention and another kind of hydrocarbon oil hydrogenation technique 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.
Hydrocarbon oil hydrogenation technique 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.
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 hydrocarbon oil hydrogenation processing flow chart of the present invention.
Among the figure: 1-fresh feed oil, 2-hydrogen, 3-first mixing tank, the 4-separating tank, 5-reactor, 6-second mixing tank, the 7-reactor feed, 8-first separator, 9-second separator, the 11-first separator waste gas, 13-solvent or thinner, 14-separating tank waste gas, the molten hydrogen turning oil of 15-, the 16-first separator separated product, 17-turning oil.
Embodiment
As shown in Figure 1, reactor shown in the figure is a two-stage catalytic agent bed.Fresh feed oil 1 mixes in first mixing tank 3 with hydrogen 2 and part turning oil in the presence of solvent or thinner 13, mixture flow enters separating tank 4, become reactor feed 7 after isolating separating tank waste gas 14, reactor feed 7 enters first section beds of reactor and catalyzer contact reacts from reactor 5 tops, another part or whole turning oil are mixed into molten hydrogen turning oil 15 with hydrogen 2 in second mixing tank 6, molten hydrogen turning oil 15 enters reactor 5 between first section of reactor 5 and second section beds, the reaction effluent separated into two parts that comes out from reactor 5 bottoms, a part is as turning oil 17, another part enters first separator 8 to be separated, isolate the first separator waste gas 11, the separated product that comes out from first separator, 8 bottoms is as the first separator separated product 16, the first separator separated product 16 enters second separator 9 again to be separated, the logistics of coming out from second separator, 9 tops is as solvent or thinner 13, and the separated product that comes out from second separator, 9 bottoms goes out device as product.17 times first mixing tanks 3 of part turning oil, another part or whole turning oil 17 enter second mixing tank 6 and are mixed into molten hydrogen turning oil 15 with hydrogen 2.
Claims (16)
1, a kind of hydrocarbon oil hydrogenation technique, it is characterized in that: hydrogen mixes the formation mixture flow with fresh feed oil and part turning oil in the presence of solvent or thinner, mixture flow enters reactor and contacts with catalyzer, another part or whole turning oil mix with hydrogen, one the tunnel or along separate routes between the reactor catalyst bed, enter reactor, a reaction effluent part is as turning oil, another part is isolated behind gas and solvent or the thinner as product, and the solubleness of hydrogen in solvent or thinner is greater than the solubleness of hydrogen in fresh feed oil and solvent or diluent mixture.
2, according to the described hydrocarbon oil hydrogenation technique of claim 1, it is characterized in that: mixture flow enters reactor from reactor top, and reaction effluent flows out from reactor lower part; Or mixture flow enters reactor from reactor lower part, and reaction effluent flows out from reactor top.
3, according to the described hydrocarbon oil hydrogenation technique of claim 1, it is characterized in that: another part or whole turning oil mix with hydrogen in the presence of solvent or thinner.
4, according to the described hydrocarbon oil hydrogenation technique of claim 1, it is characterized in that: reaction effluent is isolated behind the gas part as turning oil, and another part is isolated behind solvent or the thinner as product.
5, a kind of hydrocarbon oil hydrogenation technique, it is characterized in that: fresh feed oil with in the presence of solvent or thinner, mix the formation mixture flow after part turning oil mixes again with hydrogen, mixture flow enters reactor and contacts with catalyzer, another part or whole turning oil mix with hydrogen, one the tunnel or along separate routes between the reactor catalyst bed, enter reactor, a reaction effluent part is as turning oil, another part is isolated behind gas and solvent or the thinner as product, and the solubleness of hydrogen in solvent or thinner is greater than the solubleness of hydrogen in fresh feed oil and solvent or diluent mixture.
6, according to the described hydrocarbon oil hydrogenation technique of claim 5, it is characterized in that: mixture flow enters reactor from reactor top, and reaction effluent flows out from reactor lower part; Or mixture flow enters reactor from reactor lower part, and reaction effluent flows out from reactor top.
7, according to the described hydrocarbon oil hydrogenation technique of claim 5, it is characterized in that: another part or whole turning oil mix with hydrogen in the presence of solvent or thinner.
8, according to the described hydrocarbon oil hydrogenation technique of claim 5, it is characterized in that: reaction effluent is isolated behind the gas part as turning oil, and another part is isolated behind solvent or the thinner as product.
9, a kind of hydrocarbon oil hydrogenation technique, it is characterized in that: mix forming mixture flow after fresh feed oil, part turning oil and solvent or the mixing diluents with hydrogen, mixture flow enters reactor and contacts with catalyzer, another part or whole turning oil mix with hydrogen, one the tunnel or along separate routes between the reactor catalyst bed, enter reactor, a reaction effluent part is as turning oil, and another part is isolated behind gas and solvent or the thinner as product.
10, according to the described hydrocarbon oil hydrogenation technique of claim 9, it is characterized in that: mixture flow enters reactor from reactor top, and reaction effluent flows out from reactor lower part; Or mixture flow enters reactor from reactor lower part, and reaction effluent flows out from reactor top.
11, according to the described hydrocarbon oil hydrogenation technique of claim 9, it is characterized in that: another part or whole turning oil mix with hydrogen in the presence of solvent or thinner.
12, according to the described hydrocarbon oil hydrogenation technique of claim 9, it is characterized in that: reaction effluent is isolated behind the gas part as turning oil, and another part is isolated behind solvent or the thinner as product.
13, a kind of hydrocarbon oil hydrogenation technique, it is characterized in that: mix the formation mixture flow again with part turning oil and hydrogen after fresh feed oil and solvent or the mixing diluents, mixture flow enters reactor and contacts with catalyzer, another part or whole turning oil mix with hydrogen, one the tunnel or along separate routes between the reactor catalyst bed, enter reactor, a reaction effluent part is as turning oil, and another part is isolated behind gas and solvent or the thinner as product.
14, according to the described hydrocarbon oil hydrogenation technique of claim 13, it is characterized in that: mixture flow enters reactor from reactor top, and reaction effluent flows out from reactor lower part; Or mixture flow enters reactor from reactor lower part, and reaction effluent flows out from reactor top.
15, according to the described hydrocarbon oil hydrogenation technique of claim 13, it is characterized in that: another part or whole turning oil mix with hydrogen in the presence of solvent or thinner.
16, according to the described hydrocarbon oil hydrogenation technique of claim 13, it is characterized in that: reaction effluent is isolated behind the gas part as turning oil, and another part is isolated behind solvent or the thinner as product.
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| CN200810141293XA CN101358146B (en) | 2008-09-05 | 2008-09-05 | Hydrocarbon oil hydrogenation technique |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US9139782B2 (en) | 2011-02-11 | 2015-09-22 | E I Du Pont De Nemours And Company | Targeted pretreatment and selective ring opening in liquid-full reactors |
| US9365781B2 (en) | 2012-05-25 | 2016-06-14 | E I Du Pont De Nemours And Company | Process for direct hydrogen injection in liquid full hydroprocessing reactors |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| BR9810061B1 (en) * | 1997-06-24 | 2010-11-30 | two-phase hydroprocessing. | |
| US7569136B2 (en) * | 1997-06-24 | 2009-08-04 | Ackerson Michael D | Control system method and apparatus for two phase hydroprocessing |
| CN1464034A (en) * | 2002-06-17 | 2003-12-31 | 中国石油化工股份有限公司安庆分公司 | Process for catalyzed gasoline hydrogenation desulfurization |
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2008
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US9139782B2 (en) | 2011-02-11 | 2015-09-22 | E I Du Pont De Nemours And Company | Targeted pretreatment and selective ring opening in liquid-full reactors |
| US9365781B2 (en) | 2012-05-25 | 2016-06-14 | E I Du Pont De Nemours And Company | Process for direct hydrogen injection in liquid full hydroprocessing reactors |
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Address after: 100029 Beijing City, Chaoyang District Hui Street No. 6 Co-patentee after: Luoyang Petrochemical Engineering Corporation /SINOPEC Patentee after: China Petrochemical Group Corp. Address before: 100029 Beijing City, Chaoyang District Hui Street No. 6 Co-patentee before: Luoyang Petrochemical Engineering Co., China Petrochemical Group Patentee before: China Petrochemical Group Corp. |