CN102453528A - Multi-section boiling bed residual oil hydrogenation process method - Google Patents
Multi-section boiling bed residual oil hydrogenation process method Download PDFInfo
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Abstract
The invention discloses a multi-section boiling bed residual oil hydrogenation process method, which comprises the following steps of: mixing a hydrocarbon raw material with hydrogen, and feeding a mixture into a reactor from the bottom of a boiling bed reactor; and reacting under a hydrogenation treatment condition, wherein the boiling bed reactor comprises two or more internal circulation regions; and each internal circulation region is provided with different operation sections respectively. In the invention, a plurality of internal circulation regions are formed in the boiling bed reactor, and a plurality of different operation sections are formed, so that the entire boiling bed reactor is more flexible to operate, reasonable matching of the property of a reaction physical flow, operating conditions and catalyst performance can be realized, the activity of a catalyst is brought into full play, the yield of light oil is increased, the product quality is enhanced.
Description
Technical field
The present invention relates to a kind of multi-segment fluidized bed Residue Hydrotreating Technology method, it is interval specifically in same ebullated bed reactor, to form a plurality of different operatings, and hydrocarbon feed carries out the process method of hydrocracking between the operational zone that uses the different operating condition.
Background technology
Boiling bed hydrogenation is a gas, liquid, solid phase reaction process; Hydrocarbon feed and hydrogen mix the back and get into the pressurizing chamber of ebullated bed reactor with upflowing from reactor bottom, get into the comfort zone of ebullated bed reactor along the reactor axis gas-liquid distributing disc of upwards flowing through then.Solid catalyst particle in the reactor bed is promoted by the gas-liquid flow velocity that makes progress, and keeps granules of catalyst and is in boiling shape at random.The ideal ebullated bed reactor is full back-mixed reactors; Promptly in effective catalytic hydrocracking reaction zone; Liquid stream, gas and solid catalyst uniform distribution; Logistics in the logistics composition of reactor exit and the reactor drum is formed basic identical, so the unreacted raw material of part will be along with transforming back product outflow reactor together.Because the feed stock conversion in the full back-mixed reactors is lower; So adopt the operating method of a plurality of reactors in series usually; The catalyzer of identical or different function is seated in different reactor drums or the differential responses section of the same reactor drum that separates with dividing plate successively, to improve conversion of raw material.This will increase cost of investment, cause the irrational utilization of resource, how under lower cost, carry out boiling bed hydrogenation operation, and can improve the quality of products to greatest extent and feed stock conversion is the major issue that is worth further investigation.
US Re 25,770 has described typical liquid bed technology, and the gas-liquid logistics gets into ebullated bed reactor from reactor bottom, and axially rising along reactor drum then keeps catalyzer to be in the boiling shape, the internal recycle cup is set in the reactor drum carries out gas-liquid separation.Whole reactor is in the back-mixing state, and the entire reaction logistics transforms under the identical operations condition, so the transformation efficiency of feed stream is lower, quality product is relatively poor.
Chinese patent CN01106024.7 has introduced a kind of method for modifying that adopts liquid bed processing poor quality oil.Introduce in this invention ebullated bed reactor to be separated and form different conversion zones, the catalyst loading of different hydrogenating functions is carried out hydrogenation reaction at different conversion zones with fluid distribution dish or sieve plate.Shortcoming of the present invention is: owing to use dividing plate that reactor drum is divided into the differential responses section; Then need form effectively separating of solid and gas-liquid mixture on differential responses section top, otherwise catalyzer will block the duct on the distributing disc, this need increase separated space or set up separating device; Thereby limited the catalyzer ratio of expansion; Reduce effective catalyzed reaction space, increase operation easier, waste effective reaction volume.
Summary of the invention
Problem to the prior art existence; The present invention provides a kind of multi-segment fluidized bed Residue Hydrotreating Technology method; It is interval in the ebullated bed reactor that is provided with the internal recycle district, to form a plurality of different operatings; Reaction conditions between each operational zone is different, and this operating method can improve feed stock conversion, improves the quality of products.
Multi-segment fluidized bed Residue Hydrotreating Technology method provided by the invention comprises:
Heavy hydrocarbon feeds mixes with hydrogen from ebullated bed reactor bottom entering reactor drum, under hydroprocessing condition, reacts, and wherein said ebullated bed reactor comprises two or more internal recycle district, and different internal recycle districts adopts different operating conditions.
Described boiling bed hydrogenation reactor drum comprises the cylinder reactor housing perpendicular to ground, the triphase separator that is positioned at the housing internal upper part, guide frame and at least two internal recycle districts.Each described internal recycle district comprises cylinder, (not having the top) taper expansion section and guide frame.Said cylinder is positioned at taper expansion section top, and its lower end is connected with taper expansion section upper end.Described guide frame is the annular protrusion structure that is arranged at reactor wall, and its vertical section along reactor axis is trapezoidal or arc.The concrete structure in ebullated bed reactor and internal recycle district can be referring to the record among the applicant's the patent CN200910204287.9.According to the aspect ratio of reactor drum and the requirement of depth of conversion 2～6 internal recycle districts can be set in reactor drum, 2～3 internal recycle districts preferably are set, the barrel bore in wherein different internal recycle districts can be identical or different.Adding and decaying catalyst that live catalyst can be set respectively in different internal recycle districts are discharged parts, also can only in reactor head catalyzer be set and add parts, at reactor bottom catalyzer are set and discharge parts.
Described hydrocarbon feed can comprise any petroleum, like crude oil, straight-run gas oil, wax tailings, solvent-deasphalted oils, long residuum and vacuum residuum etc.
According to hydrogenation technique provided by the invention, different internal recycle districts forms the different operation interval in the reactor drum, and the operational condition of each reaction zone is different.Each reaction zone can use identical or different catalyzer.
In a kind of embodiment of the inventive method, according to order from bottom to top, the service temperature in each internal recycle district improves gradually, and the temperature range in adjacent internal recycle district is 5～30 ℃.The temperature of each raceway can be adjusted through any narrow fraction oil that contains the suspension bed catalyzer that injects in 300～520 ℃ of cut scopes; This distillate can be catalytic wax oil, wax tailings, the wax oil cut behind the boiling bed hydrogenation; Carbolineum in solvent-deasphalted oils and the coal tar etc.; Its IR accounts for the 5wt%～20wt% of raw material inlet amount, and the suspension bed catalyzer of use is a homogeneous catalyst known in the art, like water-soluble catalyst or oil-soluble catalyst.Water-soluble catalyst can be phosphoric acid salt or the heteropolyacid salt or the ammonia salt of nickel, molybdenum, cobalt and tungsten etc., and wherein the metal concentration of aqueous catalyst solution is 2wt%～10wt%, and the add-on of its catalyzer (by metal) accounts for 200～2000 μ g/g of distillate; Oil-soluble catalyst is many carbonyls salt or naphthenates such as nickel, molybdenum, cobalt and tungsten, and its add-on (by metal) is 200～2000 μ g/g.
The boiling bed hydrogenation reaction conditions is: reaction pressure 6～30MPa, and temperature of reaction is 350～500 ℃, air speed is 0.1～5h
-1, hydrogen to oil volume ratio is 400～3000.
According to hydrogenation technique provided by the invention, the reactive metal of boiling bed hydrogenation catalyst can be in nickel, cobalt, molybdenum or the tungsten one or more.Carrier can be in aluminum oxide, silicon oxide, aluminium oxide-silicon oxide or the titanium oxide one or more.The shape of catalyzer is extrudate or sphere.Catalyst reactor active metallic content (by weight percentage): wherein nickel or cobalt count 0.1%～10% with oxide compound, and molybdenum or tungsten count 0.5%～25% with oxide compound, and bulk density is 0.5～0.9g/cm
3, particle size (spherical diameter or bar shaped diameter) is 0.08～1.0mm, specific surface area is 80～300m
2/ g.
Multi-segment fluidized bed Residue Hydrotreating Technology of the present invention forms a plurality of internal recycle districts with different operating condition in ebullated bed reactor, the distillate that contains the suspension bed homogeneous catalyst through injection is adjusted the temperature of reaction between each operational zone.This operating method had both made the characteristics of itself and liquid bed combine closely, and can overcome the shortcoming that ebullated bed reactor exists again.As everyone knows, compare with fixed-bed reactor, ebullated bed reactor catalyzer usage quantity is few; Catalyst particles intergranular voidage is big, can process various inferior raw materials, so have the strong characteristics of adaptability to raw material; Owing to will guarantee that the catalyzer in the reactor drum is in the boiling shape, require the gas-liquid fluid to have certain LV, simultaneously so the liquid hourly space velocity of ebullated bed reactor is higher; Logistics in the ebullated bed reactor is in the back-mixing state, realizes isothermal run, can avoid the local superheating phenomenon to take place.But because catalyzer is in the boiling shape; Gas-liquid is not so good as the close fixed-bed reactor of filling mutually with the contact effect of solid catalyst; Its mass transfer effect is affected, and the liquid product of reactor outlet is second-rate, simultaneously because the back-mixing operator scheme; The raw material that part does not have enough time to react is also got rid of reactor drum along with hydrogenated products, has influenced conversion of raw material.Common ebullated bed reactor all is the isothermal operating method of single device list agent; Promptly use a kind of catalyzer in a reactor drum; Whole reactor is in uniform back-mixing state, and reactor drum is realized isothermal run, and this operator scheme is unfavorable for effective utilization of catalyzer; Limited the handiness of operation, also be unfavorable for deep hydrogenation and the conversion of reactant flow at reactor drum.Employing has the ebullated bed reactor in a plurality of internal recycle district; Different internal recycle districts adds the catalyzer and employing different operation interval of identical or different character; Can confirm The reasonable operating conditions according to logistics property and catalyst performance; Help improving the quality of products effective rate of utilization with reactor drum has increased the handiness of operation greatly.
Compared with prior art, the advantage of multi-segment fluidized bed Residue Hydrotreating Technology of the present invention is:
1, in the different internal recycle district of ebullated bed reactor, adopt different operating conditions to carry out hydrocarbon feed processing; Can logistics property and catalyst performance and operational condition be carried out rational Match; The degree of depth that realizes logistics transforms and hydro-upgrading, the utilization ratio with reaction compartment of improving the quality of products.
2, the internal recycle district that will contain 300～520 ℃ of distillates injection liquid beds of suspension bed catalyzer; Can increase light ends oil yield; The hydrogenating function of simultaneously finely divided suspension bed homogeneous catalyst can play good complementary action to boiling-bed catalyst, helps improving the hydrogenation performance and the depth of conversion of reactant flow.
3, the interval internal recycle district of a plurality of different operatings is set in ebullated bed reactor, can in reactor drum, forms a plurality of isothermal runs district, make that whole ebullated bed reactor operation is more flexible.
4, the existence in liquid bed internal recycle district has prolonged the residence time of liquid ingredient in ebullated bed reactor in the reaction back logistics, helps increasing light oil yield.
5, because ebullated bed reactor is the very high reactor drum of back-mixing degree,, a plurality of little internal recycle districts are set so usually contain the unconverted raw material of part in the reactor effluent, can conversion so that raw material repeatedly circulates, help improving transformation efficiency.
6, the internal recycle district of ebullated bed reactor is through reducing and increases the little logistics internal recycle zone that guide frame forms; It is not the different zones that strictness separates; The high activated catalyst on reactor drum top is along with the increase of metal refining and amount of coke increases its weight; Simultaneously can not satisfy the active requirement in this zone, but it can be slipped to the internal recycle district of bottom, helps making full use of of catalyst activity.
Description of drawings
Fig. 1 is the structure of reactor synoptic diagram (two internal recycle districts only are set) of a kind of embodiment of the multi-segment fluidized bed Residue Hydrotreating Technology method of the present invention.
Wherein: 1-material inlet pipe, 2-distributing disc, 3-reactor shell, 4-guide frame, 5-triphase separator inner core; 6-triphase separator urceolus, the 7-beds, the 8-targeting port, the 9-live catalyst adds pipe, 10-gas outlet pipe; The 11-triphase separator, 12-liquid outlet, 13-triphase separator catalyzer feed opening, 14-cylinder; 15-does not have addendum cone shape expansion section, 16-decaying catalyst delivery pipe, 17-internal recycle district I, 18-internal recycle district II.
Embodiment
For further setting forth concrete characteristic of the present invention, will combine accompanying drawing explanation.
In conjunction with Fig. 1, multi-segment fluidized bed residual oil reaction process method of the present invention is following:
Hot hydrocarbon feed mixes the back and gets into reactor drum by opening for feed 1 with hot hydrogen; Behind gas-liquid distributor 2, get into the effective reaction space of ebullated bed reactor; Get into thereupon near distributing disc by guide frame 4, cylinder 14 and do not have the internal recycle district 17 that addendum cone shape expansion section 15 constitutes; Logistics is pooled in cylinder 14 fluid channels through the targeting port 8 of guide frame 4 formation and the no addendum cone shape expansion section 15 of cylinder, because the cross-sectional area of fluid channel reduces at this moment, so the gas-liquid flow velocity is accelerated; Fluid is through behind the cylinder top; Fluid channel moment enlarges, and gas-liquid flow rate of flow of fluid moment reduces, and its ability of carrying solid catalyst reduces; Cause liquid and unconverted raw material and solid catalyst behind the partial reaction to flow into targeting port downwards and mix with the passage that reactor wall forms, thereby form little internal recycle district 17 from the logistics of reactor lower part to the upper reaches along cylinder outer wall.The gaseous stream and the liquid phase stream behind the partial reaction that are risen by internal recycle district 17 reach the internal recycle district 18 that catalyzer that carries on a small quantity and any narrow fraction oil of the boiling range scope that contains the suspension bed catalyzer in 300～520 ℃ that injects from targeting port are mixed into next-door neighbour's triphase separator; Above-mentioned heavy constituent and solid catalyst circulation and gaseous stream and Partial Liquid Phase logistics rising phenomenon also take place in internal recycle district 18; The logistics that wherein rises gets into triphase separator 11 through the targeting port 8 that guide frame 4 surrounds; Be separated: gas is at first separated; Discharge reactor drum through gas discharge outlet 10; The catalyzer that separates returns reaction zone through feed opening 13, and the clarified liq logistics that does not contain granules of catalyst is basically discharged reactor drums through liquid outlet 12.In order in time decaying catalyst to be discharged reactor drum and timely fresh makeup catalyst; Can the catalyzer through reactor drum top add pipe 9 fresh makeup catalyst in the reactive system, and the delivery pipe 16 through reactor lower part is with part decaying catalyst discharge reactive system.
The different internal recycle district of ebullated bed reactor of the present invention uses different operating conditions to carry out hydrogenation reaction; Wherein the operational condition of main regulation and control is temperature of reaction; Temperature of reaction difference between adjacent operational zone is controlled at 5～30 ℃; Adjust to the interval cut oil mass of injecting of different operating through control, the IR of distillate accounts for the 5wt%～20wt% of raw material usually.
The operational condition of boiling bed hydrogenation is: reaction pressure is 6～30MPa, is preferably 10～18MPa; Temperature of reaction is 350～500 ℃, is preferably 400～450 ℃; Air speed is 0.1～5h
-1, be preferably 0.5～3h
-1Hydrogen to oil volume ratio is 400～2000, is preferably 600～1500.
Two different internal recycle districts of ebullated bed reactor can use identical or different active catalyzer; If use the catalyzer of different activities; Internal recycle district from the reactor bottom to the top uses activity of such catalysts to increase successively, and the specific surface area of catalyzer increases, and granularity reduces.The activity of such catalysts metal can be in nickel, cobalt, molybdenum or the tungsten one or more.Carrier can be in aluminum oxide, silicon oxide, aluminium oxide-silicon oxide or the titanium oxide one or more.The shape of catalyzer is extrudate or sphere.Catalyst reactor active metallic content (by weight percentage): wherein nickel or cobalt count 0.1%～10% with oxide compound, and molybdenum or tungsten count 0.5%～25% with oxide compound, and bulk density is 0.5～0.9g/cm
3, particle size (spherical diameter or bar shaped diameter) is 0.08～1.0mm, specific surface area is 80～300m
2/ g.According to hydrogenation technique provided by the invention, along the engagement sequence of hydrocarbon feed and catalyzer, the particle size of catalyzer reduces 0.01～1mm in the internal recycle district, preferably reduces 0.05～0.5mm.It is 10wt%～500wt% that active metallic content in the catalyzer increases progressively ratio, preferred 50wt%～300wt%.
Further the hydrogenation effect of multi-segment fluidized bed Residue Hydrotreating Technology method of the present invention is described below in conjunction with embodiment.
Embodiment 1
Present embodiment carries out the embodiment of poor quality oil processing for using the boiling bed hydrogenation reactor drum that has two internal recycle.Wherein use the catalyzer of different hydrogenation activities respectively in two internal recycle districts; The catalyst property that uses near the internal recycle district of reactor lower part 17 with consist of: nickel 1% (calculating) by its oxide compound; Tungsten is 4% (calculating by its oxide compound), and bulk density is 0.7g/cm
3, particle diameter is 0.6mm, specific surface area is 90m
2/ g; The catalyst property that uses near internal recycle district, reactor drum top 18 with consist of: nickel 3% (calculating) by its oxide compound, molybdenum 10% (calculating) by its oxide compound, bulk density is 0.54g/cm
3, particle diameter is 0.3mm, specific surface area is 220m
2/ g.Wherein internal recycle district 17 is 1: 1 with internal recycle district 18 catalyst filling ratios, and 18 inject 350～500 ℃ the boiling bed hydrogenation distillate that contains 1000 μ g/g molybdenum naphthenates (calculating according to metal molybdenum) in the internal recycle district, and add-on accounts for the 10wt% of device inlet amount.
The feedstock property that test is used is carbon residue 18.3wt%, metal content 160 μ g/g, and bituminous matter 3wt%, S content 2.5wt%, N content 0.6wt% is with the unmanageable inferior raw material of ordinary method.
Two internal recycle districts adopt different operating conditions, and its test conditions and result see table 1.
Embodiment 2
In the present embodiment, internal recycle district 18 uses identical catalyzer with internal recycle district 17, all use use in the internal recycle district 17 catalyzer, other conditions are with embodiment 1.
Comparative example 1
This comparative example 1 is basic identical with embodiment 1, and difference is that two internal recycle districts use the identical operations condition, does not inject the distillate that contains the suspension bed catalyzer.Its reaction conditions and result see table 1.
Table 1 test conditions and test-results
Claims (15)
1. multi-segment fluidized bed Residue Hydrotreating Technology method; Comprise following content: heavy hydrocarbon feeds mixes with hydrogen from ebullated bed reactor bottom entering reactor drum; Under hydroprocessing condition, react; Wherein said ebullated bed reactor comprises two or more internal recycle district, the interval different operating conditions that adopts of different operation.
2. according to the described hydrogenation method of claim 1, it is characterized in that along reactor drum order from bottom to top, the service temperature in each internal recycle district improves gradually, the temperature range in adjacent internal recycle district is 5～30 ℃.
3. according to the described hydrogenation method of claim 1, it is characterized in that the temperature of each raceway is that 300～520 ℃ any narrow fraction oil that contains the suspension bed catalyzer is adjusted through injecting boiling range.
4. according to the described hydrogenation method of claim 3, it is characterized in that described distillate is selected from catalytic wax oil, wax tailings, boiling bed hydrogenation wax oil cut, solvent-deasphalted oils and carbolineum, its IR accounts for the 5wt%～20wt% of raw material inlet amount.
5. according to the described hydrogenation method of claim 1, it is characterized in that described ebullated bed reactor comprises 2～6 internal recycle districts, each internal recycle district comprises cylinder, no addendum cone shape expansion section and guide frame.
6. according to the described hydrogenation method of claim 5, it is characterized in that described cylinder is positioned at no addendum cone shape expansion section top, its lower end is connected with no addendum cone shape expansion section upper end.
7. according to the described hydrogenation method of claim 1, it is characterized in that the barrel bore in different internal recycle districts can be identical or different.
8. according to the described hydrogenation method of claim 7, it is characterized in that adding and decaying catalyst that live catalyst is set respectively in different internal recycle districts are discharged parts.
9. according to the described hydrogenation method of claim 1, it is characterized in that different internal recycle districts uses the catalyzer of identical activity or different activities.
10. according to the described hydrogenation method of claim 1, it is characterized in that when using the catalyzer of different activities, the internal recycle district from the reactor bottom to the top uses activity of such catalysts to increase successively, granularity reduces.
11., it is characterized in that along reactor drum order from bottom to top, the particle size of catalyzer reduces 0.01～1mm in the internal recycle district according to the described hydrogenation method of claim 10, it is 10wt%～500wt% that the active metallic content in the catalyzer increases progressively ratio.
12. according to the described hydrogenation method of claim 11; It is characterized in that; Along reactor drum order from bottom to top, the particle size of catalyzer reduces 0.05～0.5mm in the internal recycle district, and it is 50wt%～300wt% that the active metallic content in the catalyzer increases progressively ratio.
13., it is characterized in that described hydroprocessing condition is according to the described hydrogenation method of claim 1: reaction pressure 6～30MPa, temperature of reaction is 350～500 ℃, air speed is 0.1～5h
-1, hydrogen to oil volume ratio is 400～3000.
14. according to the described hydrogenation method of claim 3; It is characterized in that; Described suspension bed catalyzer is water-soluble catalyst or oil-soluble catalyst; Water-soluble catalyst is phosphoric acid salt or the heteropolyacid salt or the ammonia salt of nickel, molybdenum, cobalt and tungsten etc., and wherein the metal concentration of aqueous catalyst solution is 2wt%～10wt%; Oil-soluble catalyst is many carbonyls salt or naphthenates such as nickel, molybdenum, cobalt and tungsten.
15., it is characterized in that the add-on of described suspension bed catalyzer in distillate counted 200～2000 μ g/g with metal according to the described hydrogenation method of claim 14.
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Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104560140A (en) * | 2013-10-22 | 2015-04-29 | 中国石油化工股份有限公司 | Residual oil hydrogenation method |
| CN104560157A (en) * | 2013-10-22 | 2015-04-29 | 中国石油化工股份有限公司 | Residual oil hydrogenation method |
| CN104560137A (en) * | 2013-10-22 | 2015-04-29 | 中国石油化工股份有限公司 | Residual oil hydrogenation method |
| CN104549070B (en) * | 2013-10-12 | 2016-08-24 | 中国石油化工股份有限公司 | A kind of fluidized bed reactor |
| CN107033955A (en) * | 2017-05-27 | 2017-08-11 | 北京中科诚毅科技发展有限公司 | A kind of full plant process flow using all-round bed hydroprocessing technique |
| CN107057756A (en) * | 2017-06-23 | 2017-08-18 | 北京中科诚毅科技发展有限公司 | A kind of all-round bed hydroprocessing technique |
| CN109722281A (en) * | 2017-10-27 | 2019-05-07 | 中国石油化工股份有限公司 | The fluidized bed reactor and its method of hydrotreating recycled in one kind of multiple catalyst |
| CN112705123A (en) * | 2019-10-25 | 2021-04-27 | 中国石油化工股份有限公司 | Hydrogenation reactor and hydrogenation method |
| CN113087595A (en) * | 2020-01-08 | 2021-07-09 | 万华化学集团股份有限公司 | Method for preparing alcohol compound by hydrogenation of carbonyl-containing compound |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2187492Y (en) * | 1994-06-08 | 1995-01-18 | 天津大学 | Self-suction high-effect circular flow gas/liquid reactor |
| CN1362477A (en) * | 2001-01-05 | 2002-08-07 | 中国石油化工股份有限公司 | Hydrogenating modification method for heavy and inferior raw oil |
| CN1458234A (en) * | 2002-05-15 | 2003-11-26 | 中国石油化工股份有限公司 | Method and device for produssing residual oil |
| CN101376092A (en) * | 2007-08-27 | 2009-03-04 | 中国石油化工股份有限公司 | Novel bubbling bed reactor |
| CN102311763A (en) * | 2010-07-07 | 2012-01-11 | 中国石油化工股份有限公司 | Catalyst-graded fluidized bed hydrogenation process |
-
2010
- 2010-10-15 CN CN201010522282.3A patent/CN102453528B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2187492Y (en) * | 1994-06-08 | 1995-01-18 | 天津大学 | Self-suction high-effect circular flow gas/liquid reactor |
| CN1362477A (en) * | 2001-01-05 | 2002-08-07 | 中国石油化工股份有限公司 | Hydrogenating modification method for heavy and inferior raw oil |
| CN1458234A (en) * | 2002-05-15 | 2003-11-26 | 中国石油化工股份有限公司 | Method and device for produssing residual oil |
| CN101376092A (en) * | 2007-08-27 | 2009-03-04 | 中国石油化工股份有限公司 | Novel bubbling bed reactor |
| CN102311763A (en) * | 2010-07-07 | 2012-01-11 | 中国石油化工股份有限公司 | Catalyst-graded fluidized bed hydrogenation process |
Cited By (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104549070B (en) * | 2013-10-12 | 2016-08-24 | 中国石油化工股份有限公司 | A kind of fluidized bed reactor |
| CN104560140A (en) * | 2013-10-22 | 2015-04-29 | 中国石油化工股份有限公司 | Residual oil hydrogenation method |
| CN104560157A (en) * | 2013-10-22 | 2015-04-29 | 中国石油化工股份有限公司 | Residual oil hydrogenation method |
| CN104560137A (en) * | 2013-10-22 | 2015-04-29 | 中国石油化工股份有限公司 | Residual oil hydrogenation method |
| CN104560157B (en) * | 2013-10-22 | 2016-06-22 | 中国石油化工股份有限公司 | A kind of residual hydrogenation method |
| CN107033955A (en) * | 2017-05-27 | 2017-08-11 | 北京中科诚毅科技发展有限公司 | A kind of full plant process flow using all-round bed hydroprocessing technique |
| CN107057756A (en) * | 2017-06-23 | 2017-08-18 | 北京中科诚毅科技发展有限公司 | A kind of all-round bed hydroprocessing technique |
| CN109722281A (en) * | 2017-10-27 | 2019-05-07 | 中国石油化工股份有限公司 | The fluidized bed reactor and its method of hydrotreating recycled in one kind of multiple catalyst |
| CN109722281B (en) * | 2017-10-27 | 2020-12-08 | 中国石油化工股份有限公司 | Fluidized bed reactor with multiple catalysts for internal circulation and hydrogenation method thereof |
| CN112705123A (en) * | 2019-10-25 | 2021-04-27 | 中国石油化工股份有限公司 | Hydrogenation reactor and hydrogenation method |
| CN112705123B (en) * | 2019-10-25 | 2022-10-11 | 中国石油化工股份有限公司 | Hydrogenation reactor and hydrogenation method |
| CN113087595A (en) * | 2020-01-08 | 2021-07-09 | 万华化学集团股份有限公司 | Method for preparing alcohol compound by hydrogenation of carbonyl-containing compound |
| CN113087595B (en) * | 2020-01-08 | 2022-07-12 | 万华化学集团股份有限公司 | Method for preparing alcohol compound by hydrogenation of carbonyl-containing compound |
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