CN101993720A - Liquid phase hydrogenating method of hydrocarbon oil - Google Patents
Liquid phase hydrogenating method of hydrocarbon oil Download PDFInfo
- Publication number
- CN101993720A CN101993720A CN2009100657173A CN200910065717A CN101993720A CN 101993720 A CN101993720 A CN 101993720A CN 2009100657173 A CN2009100657173 A CN 2009100657173A CN 200910065717 A CN200910065717 A CN 200910065717A CN 101993720 A CN101993720 A CN 101993720A
- Authority
- CN
- China
- Prior art keywords
- reactor
- oil
- hydrocarbon ils
- hydrogen
- phase hydrogenatin
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Images
Abstract
The invention discloses a liquid phase hydrogenating method of hydrocarbon oil. In the method, recycle hydrogen and a recycle hydrogen compressor are cancelled; hydrogen reacts with fresh raw oil and partial recycle oil in the presence of a solvent or a diluent to form a mixture flow, and the mixture flow enters a reactor to contact with a catalyst; the other part of or all recycle oil is mixed with hydrogen, and an obtained mixture enters the reactor by a path or branches from spaces between catalyst bed layers of the reactor; partial reaction effluent is subjected to hydrogen sulfide removal and then used as recycle oil, and the other part enters a separator; and the solubility of the hydrogen in the solvent or the diluent is larger than that in the mixture of the fresh raw oil and the solvent or the diluent.
Description
Technical field
The present invention relates to hydrogen and have hydrocarbon ils processing technique field under the situation, particularly a kind of hydrocarbon ils liquid-phase hydrogenatin method.
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 the hydrocarbon oil hydrogenation process participates in reaction in fact only is useful on the hydrogen that chemical hydrogen consumes, 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 by separator and liquid phase separation and after removing impurity, by circulating hydrogen compressor its pressure is elevated to the required pressure of reaction and delivers to reactor continuation participation hydrogenation reaction, 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.
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, and suppress to generate the condensation reaction of coke.
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.
Tradition hydrogenation engineering, another purpose that adopts the exess of H2 gas is to strengthen mass transfer, takes 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, 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, with hydrogen before reactor, be dissolved in stock oil and in, 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, and its reactive behavior is lower than fresh feed, therefore the existence of turning oil has hindered contacting of stock oil and hydrogen and catalyzer, has reduced the mass transfer and the speed of response of stock oil and hydrogen.
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, and the turning oil of telling from high-pressure separator need improve temperature and deviate from contained hydrogen sulfide from entering reactor between reactor inlet or the bed.
Be that US6428686 or CN200810049938.7 do not deviate from hydrogen sulfide with the reactor outlet logistics to be recycled directly 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.
Summary of the invention
The present invention proposes a kind of hydrocarbon ils liquid-phase hydrogenatin method, deviate from the hydrogen sulfide in the turning oil, reduce its harm catalyzer.
The existence of hydrogen sulfide at first can suppress hydrodesulfurization reaction, from the reaction kinetics aspect, the hydrocarbon molecule of sulfur-bearing at first needs to be adsorbed on the activity of such catalysts center, carry out hydrogenation and desulphurization reaction then, the existence meeting of hydrogen sulfide forms absorption competition with the hydrocarbon molecule of sulfur-bearing, therefore suppresses hydrodesulfurization reaction.
A kind of hydrocarbon ils liquid-phase hydrogenatin of the present invention method is: hydrogen mixes with stock oil and part turning oil in the presence of solvent or thinner and forms 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 enter reactor between the beds, the reaction effluent part is deviate from hydrogen sulfide as turning oil through stripping, another part enters separator, hydrogen in solvent or thinner solubleness greater than the solubleness of hydrogen in stock oil and solvent or diluent mixture.
The present invention proposes another kind of hydrocarbon ils liquid-phase hydrogenatin method, stock oil forms mixture flow with mixing with hydrogen after part turning oil mixes again 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 enter reactor between the beds, the reaction effluent part is deviate from hydrogen sulfide as turning oil through stripping, another part enters separator, and the solubleness of hydrogen in solvent or thinner is greater than the solubleness of hydrogen in stock oil and solvent or diluent mixture.
The invention provides another kind of hydrocarbon ils liquid-phase hydrogenatin method, mix with hydrogen after stock 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 enter reactor between the beds, the reaction effluent part is deviate from hydrogen sulfide as turning oil through stripping, another part enters separator, and the solubleness of hydrogen in solvent or thinner is greater than the solubleness of hydrogen in stock oil and solvent or diluent mixture.
The invention provides another kind of hydrocarbon ils liquid-phase hydrogenatin method, stock oil, mix with hydrogen after 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 enter reactor between the beds, the reaction effluent part is deviate from hydrogen sulfide as turning oil through stripping, another part enters separator, utilize the amount of liquid in the content controlling reactor of hydrogen in mixture flow, the solubleness of hydrogen in solvent or thinner is greater than the solubleness of hydrogen in stock oil and solvent or diluent mixture.
The present invention proposes another kind of hydrocarbon ils liquid-phase hydrogenatin method, mix with part turning oil and hydrogen again after stock 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 enter reactor between the beds, the reaction effluent part is deviate from hydrogen sulfide as turning oil through stripping, another part enters separator, and the solubleness of hydrogen in solvent or thinner is greater than the solubleness of hydrogen in stock oil and solvent or diluent mixture.
The present invention proposes another kind of hydrocarbon ils liquid-phase hydrogenatin method, it is characterized in that: hydrogen mixes with stock oil and turning oil in the presence of solvent or thinner and forms mixture flow, mixture flow enters reactor and contacts with catalyzer, solvent or thinner mix discharge gas with hydrogen after, one the tunnel or along separate routes between the reactor catalyst bed, enter reactor, the reaction effluent part is deviate from hydrogen sulfide as turning oil through stripping, another part is isolated solvent or thinner, and isolated product liquid is as product.
The invention provides another kind of hydrocarbon ils liquid-phase hydrogenatin method, stock oil, mix with hydrogen after 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 enter reactor between the beds, the reaction effluent part is deviate from hydrogen sulfide as turning oil through stripping, another part enters separator, it is long-pending in overall reactor to contain 0.1～15 volume % gas in the reactor, and the solubleness of hydrogen in solvent or thinner is greater than the solubleness of hydrogen in stock oil and solvent or diluent mixture.
It is rare gas element or hydrogen as turning oil stripping medium that reaction effluent part of the present invention is deviate from hydrogen sulfide through stripping, preferred hydrogen, optimum is a hot high pressure hydrogen, the pressure of its hot high pressure hydrogen is higher than and stock oil and solvent or diluent mixture blended hydrogen pressure, and temperature is lower than the temperature of reaction effluent.
Mixture flow of the present invention enters reactor from reactor top, and reaction effluent flows out from reactor lower part and carries out gas-liquid separation.
Mixture flow of the present invention enters reactor from reactor lower part, and reaction effluent flows out from reactor top and carries out gas-liquid separation.
Another part of the present invention or whole turning oil mix with hydrogen in the presence of solvent or thinner.
Another part of the present invention or all turning oil in the presence of solvent or thinner, mixes with hydrogen, behind the discharge gas one the tunnel or shunt between the reactor catalyst bed, enter reactor.
Mixture flow of the present invention enters reactor after isolating gas.
Mixture flow of the present invention is mixed in mixing tank, and gas is laggard goes into reactor from going out from mixing tank top.
A kind of hydrocarbon ils liquid-phase hydrogenatin method of the present invention, described mixture flow enters reactor, and liquid contacts with catalyzer, and gas is got rid of from reactor top.
A kind of hydrocarbon ils liquid-phase hydrogenatin method of the present invention, hydrogen are mixed the formation mixture flow with stock oil and part turning oil.
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 stock oil of a kind of hydrocarbon ils liquid-phase hydrogenatin method of the present invention and another kind of hydrocarbon ils liquid-phase hydrogenatin method is the cut 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 ils liquid-phase hydrogenatin method of the present invention and another kind of hydrocarbon ils liquid-phase hydrogenatin method remove a kind of pollutent in its sulphur, nitrogen, oxygen, the metallic impurity at least, and saturated aromatic hydrocarbons, and change the molecular structure of hydrocarbon ils.
The present invention's a kind of hydrocarbon ils liquid-phase hydrogenatin method and another kind of hydrocarbon ils liquid-phase hydrogenatin method have been cancelled recycle hydrogen and circulating hydrogen compressor, utilize hydrocarbon ils, solvent or thinner that hydrogen is dissolved in wherein, for the hydrocarbon oil hydrogenation process provides hydrogen source, wherein solvent or thinner to the dissolving power of hydrogen greater than hydrocarbon ils, the addition of solvent or thinner is the amount according to the required hydrogen of hydrocarbon oil hydrogenation process reaction, and promptly chemical hydrogen consumes and regulates.
The present invention's a kind of hydrocarbon ils liquid-phase hydrogenatin method and another kind of hydrocarbon ils liquid-phase hydrogenatin method: utilize the ratio of mixture of turning oil and stock oil to control the temperature that mixture flow enters reactor, utilize the circulation oil mass controlling reactor temperature that enters between the beds.
The present invention proposes another kind of hydrocarbon ils liquid-phase hydrogenatin method, stock oil and solvent or thinner and hydrogen are mixed into mixture flow, mixture flow enters reactor and contacts with catalyzer, turning oil mixes with hydrogen in the presence of solvent or thinner, discharge behind the gas one the tunnel or between reactor inlet and beds, enter reactor along separate routes, the reaction effluent part is deviate from hydrogen sulfide as turning oil through stripping, another part enters separator, and the solubleness of hydrogen in solvent or thinner is greater than the solubleness of hydrogen in stock oil and solvent or diluent mixture.
Reaction effluent part of the present invention is deviate from hydrogen sulfide through stripping and as turning oil stripping medium is: rare gas element or hydrogen, preferred hydrogen, optimum is a hot high pressure hydrogen, the pressure of its hot high pressure hydrogen is higher than and stock oil and solvent or diluent mixture blended hydrogen pressure, and temperature is lower than the temperature of reaction effluent.
Described a kind of hydrocarbon ils liquid-phase hydrogenatin method, mixture flow enters reactor from reactor top, and reaction effluent flows out from reactor lower part.
Described a kind of hydrocarbon ils liquid-phase hydrogenatin method, mixture flow enters reactor from reactor lower part, and reaction effluent flows out from reactor top.
Described a kind of hydrocarbon ils liquid-phase hydrogenatin method, mixture flow enters reactor, and liquid contacts with catalyzer, and gas is got rid of from reactor top.
Described a kind of hydrocarbon ils liquid-phase hydrogenatin method, mixture flow enters reactor after isolating gas.
Described a kind of hydrocarbon ils liquid-phase hydrogenatin method, 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.
Catalyzer in the described a kind of hydrocarbon ils liquid-phase hydrogenatin method, reactor divides two sections fillings at least.
Described a kind of hydrocarbon ils liquid-phase hydrogenatin method, stock oil is the cut of hydrocarbon ils or hydrocarbon ils.
Described a kind of hydrocarbon ils liquid-phase hydrogenatin method stock oil is petroleum fractions, distillate, diesel oil, deasphalted oil, residual oil, lubricating oil, liquefied coal coil, shale oil or its product.
Described a kind of hydrocarbon ils liquid-phase hydrogenatin method, stock oil is deviate from a kind of of sulphur, nitrogen, oxygen and metallic impurity at least in hydrogenator, and saturated aromatic hydrocarbons.
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 the present invention's a kind of hydrocarbon ils liquid-phase hydrogenatin method and the another kind of hydrocarbon ils liquid-phase hydrogenatin method 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.
The present invention's a kind of hydrocarbon ils liquid-phase hydrogenatin method and another kind of hydrocarbon ils liquid-phase hydrogenatin method 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 hydrocarbon ils liquid-phase hydrogenatin method flow diagram of the present invention.
Fig. 2 is the another kind of hydrocarbon ils liquid-phase hydrogenatin of the present invention method flow diagram.
Fig. 3 is the third hydrocarbon ils liquid-phase hydrogenatin method flow diagram of the present invention.
Fig. 4 is the 4th kind of hydrocarbon ils liquid-phase hydrogenatin method flow diagram of the present invention.
Fig. 5 is the 5th kind of hydrocarbon ils liquid-phase hydrogenatin method flow diagram of the present invention.
Fig. 6 is the 6th kind of hydrocarbon ils liquid-phase hydrogenatin method flow diagram of the present invention.
Fig. 7 is the 7th kind of hydrocarbon ils liquid-phase hydrogenatin method flow diagram of the present invention.
Fig. 8 is the 8th kind of hydrocarbon ils liquid-phase hydrogenatin method flow diagram of the present invention.
Fig. 9 is the 9th kind of hydrocarbon ils liquid-phase hydrogenatin method flow diagram of the present invention.
Among the figure: 1-stock oil, 2-hydrogen, 3-first mixing tank, the 5-reactor, 6-second mixing tank, 7-reactor feed, 8-first separator, 9-second separator, the 11-first separator waste gas, 13-solvent or thinner, the 14-first mixing tank waste gas, the molten hydrogen turning oil of 15-, the 16-first separator charging, 17-turning oil, 18-depriving hydrogen sulphide jar, the 19-H 2 S-containing gas, the 20-second mixing tank waste gas, 21-reactor exhaust.
Embodiment
As shown in Figure 1, reactor shown in the figure is four sections beds.Stock oil 1 mixes the formation mixture flow with hydrogen 2 and part turning oil in first mixing tank 3 in the presence of partial solvent or thinner 13, mixture flow becomes reactor feed 7 isolate the first mixing tank waste gas 14 in first mixing tank 3 after, reactor feed 7 enters first section beds of reactor and catalyzer contact reacts from reactor 5 tops, another part or whole turning oil mix with hydrogen 2 in the presence of another part solvent or thinner 13 in second mixing tank 6, become molten hydrogen turning oil 15 after discharging the second mixing tank waste gas 20, molten hydrogen turning oil 15 respectively from first section of reactor 5 with second section beds, enter reactor 5 between second section and the 3rd section beds and the 3rd section and the 4th section beds, the reaction effluent that comes out from reactor 5 bottoms, the part enter depriving hydrogen sulphide jar 18 after hot high pressure hydrogen is deviate from H 2 S-containing gas 19 as turning oil 17, another part enters first separator 8 as the first separator charging 16 to be separated, isolate the first separator waste gas 11, the separated product that comes out from first separator, 8 bottoms 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.Turning oil 17 separated into two parts, a part is returned first mixing tank 3, another part or all enter second mixing tank 6.
Fig. 2, the difference of itself and Fig. 1 is: the mixture flow in first mixing tank 3 enters reactor 5 as reactor feed 7, and liquid contacts with catalyzer, and gas is got rid of from reactor 5 tops.Another part or all turning oil in second mixing tank 6 in becoming molten hydrogen turning oil 15 in the presence of another part solvent or the thinner 13 with after hydrogen 2 mixes
Fig. 3, the difference of itself and Fig. 1 is: reactor is a two-stage catalytic agent bed.Stock oil 1 forms mixture flow with mixing in first mixing tank 3 with hydrogen 2 after part turning oil mixes again in the presence of partial solvent or thinner 13.
Fig. 4, the difference of itself and Fig. 2 is: reactor is a two-stage catalytic agent bed.Stock oil 1 forms mixture flow with mixing in first mixing tank 3 with hydrogen 2 after part turning oil mixes again in the presence of partial solvent or thinner 13.
Fig. 5, it is with the difference of Fig. 1: stock oil 1, part turning oil and partial solvent or thinner 13 mix the back and mix the formation mixture flow with hydrogen 2 in first mixing tank 3.
Fig. 6, it is with the difference of Fig. 2: stock oil 1, part turning oil and partial solvent or thinner 13 mix the back and mix the formation mixture flow with hydrogen 2 in first mixing tank 3.
Fig. 7, it is with the difference of Fig. 1: stock oil 1 forms mixture flow with mixing in first mixing tank 3 with part turning oil and hydrogen 2 after partial solvent or thinner 13 mix again.
Fig. 8, it is with the difference of Fig. 2: stock oil 1 forms mixture flow with mixing in first mixing tank 3 with part turning oil and hydrogen 2 after partial solvent or thinner 13 mix again.
Fig. 9, it is with the difference of Fig. 5: stock oil 1 mixes the formation mixture flow with hydrogen 2 in first mixing tank 3 in the presence of partial solvent or thinner 13, turning oil mixes with hydrogen 2 in second mixing tank 6 with in the presence of another part solvent or the thinner 13, after discharging the second mixing tank waste gas 20, become molten hydrogen turning oil 15, molten hydrogen turning oil 15 enters reactor 5 respectively between reactor 5 inlet and first section and second section beds, second section and the 3rd section beds and the 3rd section and the 4th section beds.
Claims (66)
1. hydrocarbon ils liquid-phase hydrogenatin method, 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, reaction effluent part after stripping is deviate from hydrogen sulfide as turning oil, another part enters separator, 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 a kind of hydrocarbon ils liquid-phase hydrogenatin method of claim 1, it is characterized in that: reaction effluent part after the hot high pressure hydrogen stripped is deviate from hydrogen sulfide as turning oil.
3. according to the described a kind of hydrocarbon ils liquid-phase hydrogenatin method of claim 1, it is characterized in that: mixture flow enters reactor from reactor top, and reaction effluent flows out from reactor lower part.
4. according to the described a kind of hydrocarbon ils liquid-phase hydrogenatin method of claim 1, it is characterized in that: mixture flow enters reactor from reactor lower part, and reaction effluent flows out from reactor top.
5. according to the described a kind of hydrocarbon ils liquid-phase hydrogenatin method of claim 1, it is characterized in that: another part or whole turning oil mix with hydrogen in the presence of solvent or thinner.
6. according to the described a kind of hydrocarbon ils liquid-phase hydrogenatin method of claim 1, it is characterized in that: mixture flow is isolated and is entered reactor behind the gas and contact with catalyzer, another part or all turning oil in the presence of solvent or thinner, mixes with hydrogen, behind the discharge gas one the tunnel or shunt between the reactor catalyst bed, enter reactor.
7. according to the described a kind of hydrocarbon ils liquid-phase hydrogenatin method of claim 1, it is characterized in that: mixture flow enters reactor, and liquid contacts with catalyzer, and gas is got rid of from reactor top.
8. according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 described a kind of hydrocarbon ils liquid-phase hydrogenatin methods, it is characterized in that: hydrogen mixes the formation mixture flow with fresh feed oil and part turning oil.
9. according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 described a kind of hydrocarbon ils liquid-phase hydrogenatin methods, 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 or 3 or 4 or 5 or 6 or 7 described a kind of hydrocarbon ils liquid-phase hydrogenatin methods, it is characterized in that: the catalyzer in the reactor divides two sections fillings at least.
11. according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 described a kind of hydrocarbon ils liquid-phase hydrogenatin methods, it is characterized in that: fresh feed oil is the cut of hydrocarbon ils or hydrocarbon ils.
12. according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 described a kind of hydrocarbon ils liquid-phase hydrogenatin methods, it is characterized in that: fresh feed oil is petroleum fractions, distillate, diesel oil, deasphalted oil, residual oil, lubricating oil, liquefied coal coil, shale oil or its product.
13. according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 described a kind of hydrocarbon ils liquid-phase hydrogenatin methods, it is characterized in that: fresh feed oil is deviate from a kind of of sulphur, nitrogen, oxygen and metallic impurity at least in hydrogenator, and saturated aromatic hydrocarbons.
14. hydrocarbon ils liquid-phase hydrogenatin method, 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, the reaction effluent part is deviate from hydrogen sulfide as turning oil through stripping, another part enters separator, 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.
15., it is characterized in that according to the described a kind of hydrocarbon ils liquid-phase hydrogenatin method of claim 14: reaction effluent part after the hot high pressure hydrogen stripped is deviate from hydrogen sulfide as turning oil.
16. according to the described a kind of hydrocarbon ils liquid-phase hydrogenatin method of claim 14, it is characterized in that: mixture flow enters reactor from reactor top, and reaction effluent flows out from reactor lower part.
17. according to the described a kind of hydrocarbon ils liquid-phase hydrogenatin method of claim 14, it is characterized in that: mixture flow enters reactor from reactor lower part, reaction effluent flows out from reactor top.
18. according to the described a kind of hydrocarbon ils liquid-phase hydrogenatin method of claim 14, it is characterized in that: another part or whole turning oil mix with hydrogen in the presence of solvent or thinner.
19. according to the described a kind of hydrocarbon ils liquid-phase hydrogenatin method of claim 14, it is characterized in that: mixture flow is isolated and is entered reactor behind the gas and contact with catalyzer, another part or all turning oil in the presence of solvent or thinner, mixes with hydrogen, behind the discharge gas one the tunnel or shunt between the reactor catalyst bed, enter reactor.
20. according to the described a kind of hydrocarbon ils liquid-phase hydrogenatin method of claim 14, it is characterized in that: mixture flow enters reactor, liquid contacts with catalyzer, and gas is got rid of from reactor top.
21. according to claim 14 or 15 or 16 or 17 or 18 or 19 or 20 described a kind of hydrocarbon ils liquid-phase hydrogenatin methods, it is characterized in that: hydrogen mixes the formation mixture flow with fresh feed oil and part turning oil.
22. according to claim 14 or 15 or 16 or 17 or 18 or 19 or 20 described a kind of hydrocarbon ils liquid-phase hydrogenatin methods, 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.
23. according to claim 14 or 15 or 16 or 17 or 18 or 19 or 20 described a kind of hydrocarbon ils liquid-phase hydrogenatin methods, it is characterized in that: the catalyzer in the reactor divides two sections fillings at least.
24. according to claim 14 or 15 or 16 or 17 or 18 or 19 or 20 described a kind of hydrocarbon ils liquid-phase hydrogenatin methods, it is characterized in that: fresh feed oil is the cut of hydrocarbon ils or hydrocarbon ils.
25. according to claim 14 or 15 or 16 or 17 or 18 or 19 or 20 described a kind of hydrocarbon ils liquid-phase hydrogenatin methods, it is characterized in that: fresh feed oil is petroleum fractions, distillate, diesel oil, deasphalted oil, residual oil, lubricating oil, liquefied coal coil, shale oil or its product.
26. according to claim 14 or 15 or 16 or 17 or 18 or 19 or 20 described a kind of hydrocarbon ils liquid-phase hydrogenatin methods, it is characterized in that: fresh feed oil is deviate from a kind of of sulphur, nitrogen, oxygen and metallic impurity at least in hydrogenator, and saturated aromatic hydrocarbons.
27. hydrocarbon ils liquid-phase hydrogenatin method, it is characterized in that: fresh feed oil, mix with hydrogen after 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, the reaction effluent part is deviate from hydrogen sulfide as turning oil through stripping, another part enters separator, 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.
28., it is characterized in that according to the described a kind of hydrocarbon ils liquid-phase hydrogenatin method of claim 27: reaction effluent part after the hot high pressure hydrogen stripped is deviate from hydrogen sulfide as turning oil.
29. according to the described a kind of hydrocarbon ils liquid-phase hydrogenatin method of claim 27, it is characterized in that: mixture flow enters reactor from reactor top, and reaction effluent flows out from reactor lower part.
30. according to the described a kind of hydrocarbon ils liquid-phase hydrogenatin method of claim 27, it is characterized in that: mixture flow enters reactor from reactor lower part, reaction effluent flows out from reactor top.
31. according to the described a kind of hydrocarbon ils liquid-phase hydrogenatin method of claim 27, it is characterized in that: another part or whole turning oil mix with hydrogen in the presence of solvent or thinner.
32. according to the described a kind of hydrocarbon ils liquid-phase hydrogenatin method of claim 27, it is characterized in that: mixture flow is isolated and is entered reactor behind the gas and contact with catalyzer, another part or all turning oil in the presence of solvent or thinner, mixes with hydrogen, behind the discharge gas one the tunnel or shunt between the reactor catalyst bed, enter reactor.
33. according to the described a kind of hydrocarbon ils liquid-phase hydrogenatin method of claim 27, it is characterized in that: mixture flow enters reactor, liquid contacts with catalyzer, and gas institute body is got rid of from reactor top.
34. according to claim 27 or 28 or 29 or 30 or 31 or 32 or 33 described a kind of hydrocarbon ils liquid-phase hydrogenatin methods, it is characterized in that: hydrogen mixes the formation mixture flow with fresh feed oil and part turning oil.
35. according to claim 27 or 28 or 29 or 30 or 31 or 32 or 33 described a kind of hydrocarbon ils liquid-phase hydrogenatin methods, 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.
36. according to claim 27 or 28 or 29 or 30 or 31 or 32 or 33 described a kind of hydrocarbon ils liquid-phase hydrogenatin methods, it is characterized in that: the catalyzer in the reactor divides two sections fillings at least.
37. according to claim 27 or 28 or 29 or 30 or 31 or 32 or 33 described a kind of hydrocarbon ils liquid-phase hydrogenatin methods, it is characterized in that: fresh feed oil is the cut of hydrocarbon ils or hydrocarbon ils.
38. according to claim 27 or 28 or 29 or 30 or 31 or 32 or 33 described a kind of hydrocarbon ils liquid-phase hydrogenatin methods, it is characterized in that: fresh feed oil is petroleum fractions, distillate, diesel oil, deasphalted oil, residual oil, lubricating oil, liquefied coal coil, shale oil or its product.
39. according to claim 27 or 28 or 29 or 30 or 31 or 32 or 33 described a kind of hydrocarbon ils liquid-phase hydrogenatin methods, it is characterized in that: fresh feed oil is deviate from a kind of of sulphur, nitrogen, oxygen and metallic impurity at least in hydrogenator, and saturated aromatic hydrocarbons.
40. hydrocarbon ils liquid-phase hydrogenatin method, 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, the reaction effluent part is deviate from hydrogen sulfide as turning oil through stripping, another part enters separator, 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.
41. according to the described a kind of hydrocarbon ils liquid-phase hydrogenatin method of claim 40, it is characterized in that: the reaction effluent part is deviate from hydrogen sulfide as turning oil through the hot high pressure hydrogen stripped.
42. according to the described a kind of hydrocarbon ils liquid-phase hydrogenatin method of claim 40, it is characterized in that: mixture flow enters reactor from reactor top, and reaction effluent flows out from reactor lower part.
43. according to the described a kind of hydrocarbon ils liquid-phase hydrogenatin method of claim 40, it is characterized in that: mixture flow enters reactor from reactor lower part, reaction effluent flows out from reactor top.
44. according to the described a kind of hydrocarbon ils liquid-phase hydrogenatin method of claim 40, it is characterized in that: another part or whole turning oil mix with hydrogen in the presence of solvent or thinner.
45. according to the described a kind of hydrocarbon ils liquid-phase hydrogenatin method of claim 40, it is characterized in that: mixture flow is isolated and is entered reactor behind the gas and contact with catalyzer, another part or all turning oil in the presence of solvent or thinner, mixes with hydrogen, behind the discharge gas one the tunnel or shunt between the reactor catalyst bed, enter reactor.
46. according to the described a kind of hydrocarbon ils liquid-phase hydrogenatin method of claim 40, it is characterized in that: mixture flow enters reactor, liquid contacts with catalyzer, and gas is got rid of from reactor top.
47. according to claim 40 or 41 or 42 or 43 or 44 or 45 or 46 described a kind of hydrocarbon ils liquid-phase hydrogenatin methods, it is characterized in that: hydrogen mixes the formation mixture flow with fresh feed oil and part turning oil.
48. according to claim 40 or 41 or 42 or 43 or 44 or 45 or 46 described a kind of hydrocarbon ils liquid-phase hydrogenatin methods, 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.
49. according to claim 40 or 41 or 42 or 43 or 44 or 45 or 46 described a kind of hydrocarbon ils liquid-phase hydrogenatin methods, it is characterized in that: the catalyzer in the reactor divides two sections fillings at least.
50. according to claim 40 or 41 or 42 or 43 or 44 or 45 or 46 described a kind of hydrocarbon ils liquid-phase hydrogenatin methods, it is characterized in that: fresh feed oil is the cut of hydrocarbon ils or hydrocarbon ils.
51. according to claim 40 or 41 or 42 or 43 or 44 or 45 or 46 described a kind of hydrocarbon ils liquid-phase hydrogenatin methods, it is characterized in that: fresh feed oil is petroleum fractions, distillate, diesel oil, deasphalted oil, residual oil, lubricating oil, liquefied coal coil, shale oil or its product.
52. according to claim 40 or 41 or 42 or 43 or 44 or 45 or 46 described a kind of hydrocarbon ils liquid-phase hydrogenatin methods, it is characterized in that: fresh feed oil is deviate from a kind of of sulphur, nitrogen, oxygen and metallic impurity at least in hydrogenator, and saturated aromatic hydrocarbons.
53. hydrocarbon ils liquid-phase hydrogenatin method, it is characterized in that: fresh feed oil and solvent or thinner and hydrogen are mixed into mixture flow, mixture flow enters reactor and contacts with catalyzer, turning oil mixes with hydrogen in the presence of solvent or thinner, discharge behind the gas one the tunnel or between reactor inlet and beds, enter reactor along separate routes, the reaction effluent part is deviate from hydrogen sulfide as turning oil through stripping, another part enters separator, 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.
54. according to the described a kind of hydrocarbon ils liquid-phase hydrogenatin method of claim 53, it is characterized in that: the reaction effluent part is deviate from hydrogen sulfide as turning oil through the hot high pressure hydrogen stripped.
55. according to the described a kind of hydrocarbon ils liquid-phase hydrogenatin method of claim 53, it is characterized in that: mixture flow enters reactor from reactor top, and reaction effluent flows out from reactor lower part.
56. according to the described a kind of hydrocarbon ils liquid-phase hydrogenatin method of claim 53, it is characterized in that: mixture flow enters reactor from reactor lower part, reaction effluent flows out from reactor top.
57. according to the described a kind of hydrocarbon ils liquid-phase hydrogenatin method of claim 53, it is characterized in that: mixture flow enters reactor, liquid contacts with catalyzer, and gas is got rid of from reactor top.
58. according to the described a kind of hydrocarbon ils liquid-phase hydrogenatin method of claim 53, it is characterized in that: mixture flow enters reactor after isolating gas.
59. according to claim 53 or 54 or 55 or 56 or 57 or 58 described a kind of hydrocarbon ils liquid-phase hydrogenatin methods, 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.
60. according to claim 53 or 54 or 55 or 56 or 57 or 58 described a kind of hydrocarbon ils liquid-phase hydrogenatin methods, it is characterized in that: the catalyzer in the reactor divides two sections fillings at least.
61. according to claim 53 or 54 or 55 or 56 or 57 or 58 described a kind of hydrocarbon ils liquid-phase hydrogenatin methods, it is characterized in that: fresh feed oil is the cut of hydrocarbon ils or hydrocarbon ils.
62. according to claim 53 or 54 or 55 or 56 or 57 or 58 described a kind of hydrocarbon ils liquid-phase hydrogenatin methods, it is characterized in that: fresh feed oil is petroleum fractions, distillate, diesel oil, deasphalted oil, residual oil, lubricating oil, liquefied coal coil, shale oil or its product.
63. according to claim 53 or 54 or 55 or 56 or 57 or 58 described a kind of hydrocarbon ils liquid-phase hydrogenatin methods, it is characterized in that: fresh feed oil is deviate from a kind of of sulphur, nitrogen, oxygen and metallic impurity at least in hydrogenator, and saturated aromatic hydrocarbons.
64. hydrocarbon ils liquid-phase hydrogenatin method, it is characterized in that: hydrogen mixes the formation mixture flow with fresh feed oil and turning oil in the presence of solvent or thinner, mixture flow enters reactor and contacts with catalyzer, solvent or thinner mix discharge gas with hydrogen after, one the tunnel or along separate routes between the reactor catalyst bed, enter reactor, the reaction effluent part is deviate from hydrogen sulfide as turning oil through stripping, another part is isolated solvent or thinner, and isolated product liquid is as product.
65. hydrocarbon ils liquid-phase hydrogenatin method, fresh feed oil, mix with hydrogen after 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 enter reactor between the beds, the reaction effluent part is deviate from hydrogen sulfide as turning oil through stripping, another part enters separator, utilize the amount of liquid in the content controlling reactor of hydrogen in mixture flow, the solubleness of hydrogen in solvent or thinner is greater than the solubleness of hydrogen in fresh feed oil and solvent or diluent mixture.
66. hydrocarbon ils liquid-phase hydrogenatin method, fresh feed oil, mix with hydrogen after 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 enter reactor between the beds, the reaction effluent part is deviate from hydrogen sulfide as turning oil through stripping, another part enters separator, it is long-pending in overall reactor to contain 0.1～15 volume % gas in the reactor, 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.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009100657173A CN101993720A (en) | 2009-08-11 | 2009-08-11 | Liquid phase hydrogenating method of hydrocarbon oil |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009100657173A CN101993720A (en) | 2009-08-11 | 2009-08-11 | Liquid phase hydrogenating method of hydrocarbon oil |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN101993720A true CN101993720A (en) | 2011-03-30 |
Family
ID=43784486
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2009100657173A Pending CN101993720A (en) | 2009-08-11 | 2009-08-11 | Liquid phase hydrogenating method of hydrocarbon oil |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101993720A (en) |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102732298A (en) * | 2011-04-12 | 2012-10-17 | 中国石油化工股份有限公司 | Liquid phase hydrogenation method |
| CN103224809A (en) * | 2013-04-27 | 2013-07-31 | 中国海洋石油总公司 | Method for producing clean oil product through liquid-phase product cyclic hydrogenation |
| CN107267198A (en) * | 2017-08-11 | 2017-10-20 | 南京康鑫成生物科技有限公司 | A kind of method that waste lubricating oil liquid-phase hydrogenatin prepares lube base oil |
| CN108003924A (en) * | 2016-11-01 | 2018-05-08 | 中国石油化工股份有限公司 | Improve the Heavy oil hydrogenation method of catalyst utilization |
| CN108003919A (en) * | 2016-11-01 | 2018-05-08 | 中国石油化工股份有限公司 | A kind of heavy oil hydrogenation treatment method for lifting catalyst utilization |
| CN108018084A (en) * | 2016-11-01 | 2018-05-11 | 中国石油化工股份有限公司 | A kind of heavy oil hydrogenation treatment method for improving catalyst utilization |
| CN108018074A (en) * | 2016-11-01 | 2018-05-11 | 中国石油化工股份有限公司 | Improve the heavy oil hydrogenation treatment method of catalyst utilization |
| CN109777505A (en) * | 2017-11-14 | 2019-05-21 | 中国石油化工股份有限公司 | REFINERY GAS combined method |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1040612A (en) * | 1988-08-11 | 1990-03-21 | 国际壳牌研究有限公司 | The process for hydrocracking of hydrocarbonaceous of hydrocarbon feed |
| CN1051751A (en) * | 1989-11-16 | 1991-05-29 | 国际壳牌研究有限公司 | Transform the processing method of hydrocarbon ils |
| CN1226920A (en) * | 1996-08-01 | 1999-08-25 | 国际壳牌研究有限公司 | Hydrotreating process |
| US7291257B2 (en) * | 1997-06-24 | 2007-11-06 | Process Dynamics, Inc. | Two 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 |
| US20090095651A1 (en) * | 2007-10-15 | 2009-04-16 | Laura Elise Leonard | Hydrocarbon Conversion Process |
-
2009
- 2009-08-11 CN CN2009100657173A patent/CN101993720A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1040612A (en) * | 1988-08-11 | 1990-03-21 | 国际壳牌研究有限公司 | The process for hydrocracking of hydrocarbonaceous of hydrocarbon feed |
| CN1051751A (en) * | 1989-11-16 | 1991-05-29 | 国际壳牌研究有限公司 | Transform the processing method of hydrocarbon ils |
| CN1226920A (en) * | 1996-08-01 | 1999-08-25 | 国际壳牌研究有限公司 | Hydrotreating process |
| US7291257B2 (en) * | 1997-06-24 | 2007-11-06 | Process Dynamics, Inc. | Two phase hydroprocessing |
| US20090095651A1 (en) * | 2007-10-15 | 2009-04-16 | Laura Elise Leonard | Hydrocarbon Conversion Process |
| 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 (14)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102732298A (en) * | 2011-04-12 | 2012-10-17 | 中国石油化工股份有限公司 | Liquid phase hydrogenation method |
| CN103224809A (en) * | 2013-04-27 | 2013-07-31 | 中国海洋石油总公司 | Method for producing clean oil product through liquid-phase product cyclic hydrogenation |
| CN103224809B (en) * | 2013-04-27 | 2014-12-03 | 中国海洋石油总公司 | Method for producing clean oil product through liquid-phase product cyclic hydrogenation |
| CN108003919B (en) * | 2016-11-01 | 2020-10-16 | 中国石油化工股份有限公司 | Heavy oil hydrotreating method for improving catalyst utilization rate |
| CN108003924A (en) * | 2016-11-01 | 2018-05-08 | 中国石油化工股份有限公司 | Improve the Heavy oil hydrogenation method of catalyst utilization |
| CN108003919A (en) * | 2016-11-01 | 2018-05-08 | 中国石油化工股份有限公司 | A kind of heavy oil hydrogenation treatment method for lifting catalyst utilization |
| CN108018084A (en) * | 2016-11-01 | 2018-05-11 | 中国石油化工股份有限公司 | A kind of heavy oil hydrogenation treatment method for improving catalyst utilization |
| CN108018074A (en) * | 2016-11-01 | 2018-05-11 | 中国石油化工股份有限公司 | Improve the heavy oil hydrogenation treatment method of catalyst utilization |
| CN108018084B (en) * | 2016-11-01 | 2020-10-16 | 中国石油化工股份有限公司 | Heavy oil hydrotreating method for improving catalyst utilization rate |
| CN108018074B (en) * | 2016-11-01 | 2020-10-16 | 中国石油化工股份有限公司 | Heavy oil hydrotreating method for improving catalyst utilization rate |
| CN108003924B (en) * | 2016-11-01 | 2020-10-16 | 中国石油化工股份有限公司 | Heavy oil hydrogenation method for improving catalyst utilization rate |
| CN107267198A (en) * | 2017-08-11 | 2017-10-20 | 南京康鑫成生物科技有限公司 | A kind of method that waste lubricating oil liquid-phase hydrogenatin prepares lube base oil |
| CN109777505A (en) * | 2017-11-14 | 2019-05-21 | 中国石油化工股份有限公司 | REFINERY GAS combined method |
| CN109777505B (en) * | 2017-11-14 | 2021-01-05 | 中国石油化工股份有限公司 | Refinery gas hydrogenation combination method |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN201644076U (en) | Liquid-phase hydrogenated reactor | |
| CN101280217A (en) | Liquid-solid two-phase hydrogenation method for hydrocarbon oil | |
| CN101993720A (en) | Liquid phase hydrogenating method of hydrocarbon oil | |
| KR102529349B1 (en) | Method for converting feedstocks comprising a hydrotreatment step, a hydrocracking step, a precipitation step and a sediment separation step, in order to produce fuel oils | |
| CN101992048A (en) | Reactor and application thereof to hydrocarbon oil liquid-solid two-phase hydrogenation | |
| CN101875855B (en) | Method for hydrogenation and catalytic cracking of residual oil | |
| CN102732298A (en) | Liquid phase hydrogenation method | |
| CN101760233A (en) | Method for hydrocracking of coked wax oil | |
| CN101107060A (en) | Hydrocracking method of heavy feedstocks with improved hydrogen processing | |
| CN101338219A (en) | Two-phase hydrogenation process | |
| CN101381623B (en) | Liquid-solid two-phase hydrogenation method | |
| CN101275083A (en) | Hydrogenation method for hydrocarbon oils | |
| CN101376841B (en) | Heavy fraction oil hydrotreating method | |
| CN101280218A (en) | Two-phase hydrogenation method for hydrocarbon oil | |
| CN101280219A (en) | Two-phase hydrogenation method for hydrocarbon oil | |
| US20040188328A1 (en) | Combined hydrotreating and process | |
| CN108949227A (en) | A kind of high nitrogen multistage containing aromatic naphtha adds hydrogen formula advanced nitrogen deeply de-aromatizing method | |
| CN202063881U (en) | Liquid-phase hydrogenation reactor | |
| CN101434867A (en) | Suspension bed residual oil hydrogenation-catalytic cracking combined technological process | |
| CN101376840A (en) | Heavy fraction oil hydrotreating method | |
| CN102634367A (en) | Double-phase hydrogenating method | |
| CN101358146B (en) | Hydrocarbon oil hydrogenation technique | |
| CN102618320B (en) | Method for biphase hydrogenation of hydrocarbon oil | |
| CN101993719A (en) | Method for hydrogenating hydrocarbon oil and reactor thereof | |
| CN101338220A (en) | Hydrogenation method for hydrocarbon oils |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C53 | Correction of patent of invention or patent application | ||
| CB02 | Change of applicant information |
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 |
|
| C12 | Rejection of a patent application after its publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20110330 |