CN1251794C - Operating method for fixed bed gas-liquid counter current reactor - Google Patents
Operating method for fixed bed gas-liquid counter current reactor Download PDFInfo
- Publication number
- CN1251794C CN1251794C CN 03133565 CN03133565A CN1251794C CN 1251794 C CN1251794 C CN 1251794C CN 03133565 CN03133565 CN 03133565 CN 03133565 A CN03133565 A CN 03133565A CN 1251794 C CN1251794 C CN 1251794C
- Authority
- CN
- China
- Prior art keywords
- catalyst
- liquid
- bed
- gas
- configuration
- 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.)
- Expired - Lifetime
Links
Images
Abstract
The present invention relates to an operation method for a gas-liquid counterflow reactor of a fixed bed. A gas-liquid counterflow contact bed with three-stage catalyst pore canals is formed by changing and optimizing the source and the distribution of pore canals inside a catalyst (or filling material) bed. The gas-liquid counterflow contact bed is filled in a clutter method; the void ratio of the bed is from 0.40 to 0.95; one kind or many kinds of catalysts are used; at least one kind of catalyst granules have conformation with high void ratio; 10 to 90% of the void ratio of the bed is derived from the granules. The method of the present invention effectively solves the problem of liquid flooding and increases the stability and the flexibility of operation. The source, the proportion and the configuration of three-stage bed pore canals are configured and optimized to make fluid of a gas phase and a liquid phase uniformly distributed; the mass transfer is strengthened, and the reaction efficiency is increased. The method of the present invention is mainly used for processes of the catalytic reaction or the physical separation, etc. of gas, liquid and solid countercurrent contact in the technical fields of petroleum refining, organic chemical industry, environmental treatment, etc.
Description
Technical field
The present invention relates to the method for operating of processes such as the gas, liquid, solid three-phase counter-current contact catalysis reaction of a kind of method of operating of fixed bed gas-liquid counter current reactor, particularly technical field such as petroleum refining, organic chemical industry or physical separation.
Background technology
In gas, liquid contact physics or the chemical reaction process of catalyst or filler existence, gas, the liquid type of flow adopt two kinds usually, and a kind of is gas, liquid also stream mode in the same way, and another is the reverse reflux type of gas, liquid.For the counter-current operation mode, stable operation (liquid flooding does not take place) mass-transfer efficiency gentle, the liquid two-phase is two emphasis Considerations, may become the key factor of decision technological feasibility sometimes.
Control liquid flooding major measure is the shape that changes catalyst in the prior art, or the type of feed of change catalyst granules, make gas phase and liquid phase be similar in different passages and flow, thus the interaction of minimizing gas-liquid two-phase, be skin friction resistance, suppress the generation of liquid flooding.
IFM reactor (The internally finned monolith reactor) (Chem EngSci, 1997,52 (21/22): 3893-3899) inner catalyst layer is not to be formed by the catalyst granules filling, but form by the multi beam pipeline of catalyst configuration, each pipeline inner wall all is inserted with the catalyst longitudinal fin of some.Liquid phase can be owing to capillary effect in this adverse current phase reactor, and the recess in pipeline between each fin flows downward with the form of fluctuation circular membrane stream; And gas phase is because the pressure drop effect, and upwards flow in the core place in pipeline.This reactor exists the geometry of liquid phase outlet to produce the gas phase that enters pipeline to disturb, thereby makes gas phase skewness in each pipeline, and and then influences the shortcoming of initial liquid flooding condition.
Catalyst is seated in phase reactor (Chem EngSci, 1999, the 54:1339-1345 in the regular katapak-s catalytic filler; Chem Eng Sci, 1999,54:1367-1374; Chem EngSci, 1999,54:5145-5152).Catalyst is seated in the regular katapak-s filler.Have two kinds of passages in the reactor, a kind of is the filler passage (packed channels) that is filled with catalyst granules, and another kind is the open channels (open channels) of not loading catalyst granules.The superficial liquid velocity of this type of reactor has a critical value.When superficial liquid velocity during less than critical value, the liquid phase main body flows in filler passage; When superficial liquid velocity when critical, the liquid holdup in the filler passage reaches maximum, then liquid phase not only flows in filler passage, also can flow in open channels, has good interchange reaction between the mobile liquid phase in these two passages.The gas phase main body flows in open channels.This reactor has the advantage of good radially liquid distribution, but also exists katapak-s filler price expensive, is not suitable for the shortcoming of commercial Application.
TLP reactor (The three-levels-of-porosity reactor) (Chem.Eng.Sci., 1997,52:3901-3907; Chem Eng Sci, 1999,54:1405-1411; Chem EngSci, 1999,54:3701-3708; Chem Eng Sci, 1999,54:5047-5053).The TLP reactor is made of woven wire basket layer, and the blue basket number that each layer has can be identical, also can be different.Catalyst granules is seated in the wire basket with netting on top basket.Have three kinds of holes in the packing layer: the hole of catalyst particles intragranular is a micron order; The hole of catalyst particles intergranular is the millimeter level; With in the blue basket layer of one deck between each blue basket and blue basket layer with layer between hole be Centimeter Level.Liquid phase in such reactor can flow downward by the millimeter grade hole crack between the catalyst granules in the blue basket under the gravity effect; Gas phase is upwards flowing by the Centimeter Level hole between the blue basket under the effect of pressure drop.This reactor has gas phase and liquid phase and is similar in the different passages and flows, so influencing each other between the gas-liquid two-phase is less, the apparent small increase that only causes pressure to fall for high liquid speed, and high gas speed only causes the advantage of the small increase of liquid holdup.But also exist because liquid phase trends towards attached to blue basket bottom, promptly under flowing to before one deck liquid phase assemble in blue basket minimum point, thereby the shortcoming that causes liquid distribution on the liquid flow path direction, to worsen.Another weak point of above-mentioned beds type of feed is that fluid flowing passage is bigger, and fluid distribution and reallocation property are bad, and mass-transfer efficiency is low, and the space reactor utilization rate is low.
Along with the increase day by day to the clean fuel demand, the advanced Clean Fuel Production technology of exploitation becomes the current important subject in each oil company, the world.Up to now, catalytic hydrogenation remains the effective technology of producing clean fuel.But clean fuel specification requirement now is more and more higher, adopt common hydrogen addition technology also difficulty satisfy market demands.Reason is that the hydrogenation technique flow process of routine at present all is to flow through the solid catalyst bed layer under raw material and the hydrogen and the flow direction, and the reaction logistics is with the gas and liquid flowing technology of advancing, going out together.There is following shortcoming in this type of technology: the heat release meeting of (1) hydrogenation reaction raises the reaction system temperature and causes a large amount of liquid hydrocarbon vaporizations, influences the concentration of hydrogen in the reactor; (2) the heat release meeting of hydrogenation reaction causes more near reactor outlet, and the reaction stream temperature is high more, and it is unfavorable that diesel oil deep is taken off virtue; In actual diesel oil fraction hydrogenating subtractive process, thermodynamical equilibrium can limit the saturated further reaction of aromatic hydrogenation; (3) because the gas-liquid two-phase concurrent flow, is reacted logistics by beds with advancing with going out the H that causes reaction to generate
2S and NH
3Be trapped in the reaction system always, thus strong inhibition desulfurization take off further carrying out of arylation reaction.And the vapour-liquid countercurrent reaction can effectively address the above problem, and therefore, the gas-liquid counter current hydrogenation technique becomes the research emphasis of each oil company, the world.
At present, the diesel oil hydrofining reactor all is the function catalyst that the simple function beds adopts single type, it is seated in forms a beds together.And reaction is carried out under liquid phase state, for guaranteeing the catalyst efficiency factor, can only adopt catalyst particle.In addition,, be in again in the soaked with liquid, can only adopt solid construction could guarantee catalyst strength because beds is very high.Therefore, the catalyst of commercial Application all is following sphere or a bar shaped catalyst of particle diameter 3mm, and this type of beds voidage is 0.35-0.45, and is more much smaller than the voidage (＞0.95) of the counter-current operation of routine.If the reactor at big or small like this bed voidage carries out counter-current operation, easily produce liquid flooding, cause the device running unstable.
USP 5,985, and 131, proposition such as USP 6,007,787 adopts the method for gas bypassing to avoid liquid flooding.Though this method can reduce the liquid holdup of reactor, its essence is and reduced gas flow, promptly reduce the gas-liquid ratio of knowing clearly, must influence the end reaction effect.And for the high-quality clean fuel, for guaranteeing its hydrogenation degree of depth, certain hydrogen oil (gas-liquid) ratio is the operating condition that must lack.Then there is above-mentioned corresponding problem in three kinds of reactors such as above-mentioned IFM if be used for the diesel oil hydrogenation process, the most important thing is that wherein its gas-liquid mass transfer efficient is low, can not finish the deep hydrofinishing reaction.
Summary of the invention
At the problem that prior art exists, the purpose of this invention is to provide a kind of flow operation method of gas, liquid, solid three-phase back reaction device, realize stable, the flexible operating of gas-liquid counter current, and can improve mass-transfer efficiency, improve the utilization rate of space reactor.The inventive method can be used for various gas, liquid adverse current physics or chemical reaction processes with solid catalyst or filler.
Gas, liquid, solid three-phase counter-current reactor method of operating of the present invention is included on catalyst (or filler) bed, gas phase and liquid phase reverse flow, the gas, liquid, solid three-phase contacts with each other material Transfer or chemical reaction takes place, main inventive point is source and the distribution by the duct that changes, optimizes catalyst (or filler) bed inside, forms a kind of gas-liquid counter current contact bed with three grades of catalyst (or filler) duct.Concrete scheme is: catalyst (or filler) employing huddles mode and loads, and the voidage of bed is generally 0.40～0.95, is preferably 0.45～0.80.Catalyst (or filler) can adopt one or more, select for use 1～5 kind can satisfy common physics or chemical process generally speaking, certainly can select more catalyst or filler for use according to particular case, wherein have at least a kind of catalyst (or filler) particle to have catalyst (or filler) particle of high voidage configurations such as groove, duct, the voidage with high voidage configuration particle itself is 0.10～0.95.The space of particle own accounts for 10～90% of bed space.
Illustrate: the voidage of particle own is meant that particle surface or the inner isostructural space of groove, hole account for the ratio of particle gross space (space that the particle entity occupies and the spacial summation of structures such as groove, hole are the not volume of with groove column of the identical and length of diameter as the particle gross space of with groove column).The ratio that the space of particle own accounts for the bed space is the ratio that the own space of particle of calculating accounts for the bed space of actual measurement.
The inventive method generally can adopt the following realization of following concrete technical scheme: (1) uses the catalyst (or filler) of high voidage configuration to huddle filling formation three grades of duct catalyst (or filler) bed; (2) with the catalyst (or filler) and high voidage configuration catalyst (or filler) of conventional configuration, huddle filling after the mixing, constitute three grades of duct catalyst (or filler) bed.The granularity of various catalyst (or filler) can be identical or different.
Above-mentioned three grades of duct beds are meant that the lyriform pore road, space that is had in catalyst (or filler) bed is three kinds of dissimilar, separate sources, the not duct or the space of same-action: have nanoscale and/or micron order duct in catalyst (or filler) particle; Have millimeter grade hole road or space between catalyst (or filler) particle; Catalyst (or filler) particle originally also has millimetre-sized duct or groove on one's body.Intragranular duct is the main place of physics or chemical reaction, can select the catalyst or the filler in suitable duct according to different physics or chemical process.Duct between the duct of particle itself or groove and a material or space are the mobile passages that reaches external diffusion of gas-liquid two-phase, and the mass-transfer efficiency of gas-liquid two-phase is had material impact.
Factors such as the material character of the formation in three grades of ducts and catalyst (or filler), granular size, particle configuration, mixed type are relevant, can be according to different physics or chemical reaction system, optimize the structure in ratio, separate sources duct in separate sources duct in three grades of ducts and distribution etc., to adapt to different processes.
The configuration of high voidage configuration catalyst of the present invention is meant that particle outer surface or inside have the catalyst shape of millimeter grade hole road or groove, as two leaf posts, three leaf posts, four leaf posts, annular, Raschig ring, butterfly etc., certainly the rib of leaf cylindricality catalyst can be symmetry also can be asymmetric.The shape of the function catalyst of conventional configuration can be spherical, cylindricality, clover, bunge bedstraw herb etc., for the voidage that increases beds with improve transmittance process between the gas-liquid-solid three-phase, can be the shape of above-mentioned high voidage configuration catalyst with the inert filler of the function catalyst mix of conventional configuration filling or the configuration of catalyst, also can be other catalyst shape with millimeter level groove or duct, both mixed proportions can freely be adjusted according to the feedstock oil character of being processed (mainly being density and viscosity) and the operating condition of reactor, less as feedstock oil viscosity, the mixed proportion of the big then high voidage configuration catalyst of density is less, otherwise then big.
Described high voidage configuration size of catalyst is: two leaf posts, three leaf posts, four leaf column diameters are generally 1.5mm～15.0mm, length is 2.0～15.0mm, the general diameter 8～50mm of annular, length is 8～50mm, and the size of other shaped particles such as Raschig ring can be selected the size of various criterion specification for use according to the device needs.The conventional catalyst configuration is of a size of: spherical diameter is generally 1.0mm～3.0mm, and the diameter of cylindricality, clover, bunge bedstraw herb is generally 1.0mm～2.5mm, and length is 3.0～8.0mm.
For different practical situations; above-mentioned various factors can be optimized and revised; as for diesel oil countercurrent hydrogenation technology; catalyst can be selected catalyst for hydrogenation treatment of diesel oil; material is generally aluminium oxide; sial; porous refractory thing and active metal components such as molecular sieve; the duct of catalyst inside is based on the nanoscale duct; it is that 2～4mm length is the different cylindricality that 4～10mm outer surface has 0.2～1.5mm groove that the particle configuration can adopt diameter; as three leaf posts; four Ye Zhu etc.; also can adopt different cylindricality and conventional configuration particle mixed packing; the voidage of particle itself is 0.20～0.85, is preferably 0.25～0.55.The bed voidage that huddles after the filling is 0.45～0.85, is preferably 0.50～0.75, and the space of control particle own accounts for 30～80% of bed space.Mixing the conventional catalyst configuration that uses is of a size of: spherical diameter is generally 1.0mm～3.0mm, and the diameter of cylindricality, clover, bunge bedstraw herb is generally 1.0mm～2.5mm, and length is 3.0～8.0mm.The process conditions of diesel oil countercurrent hydrogenation are generally: 200～427 ℃ of reaction temperatures; Reaction pressure is 1.0～20.0MPa; Hydrogen to oil volume ratio is 50～1000; Volume space velocity is 0.1-10.0h during liquid
-1Be preferably: 200～380 ℃ of reaction temperatures; Reaction pressure is 3.0～12.0MPa; Hydrogen to oil volume ratio is 50～500; Volume space velocity is 0.5-7.5h during liquid
-1
The inventive method can be used for variously having solid catalyst or filler to exist under the situation, the physics or the chemical reaction process of gas-liquid counter current operation.As go for all kinds of diesel oil deep hydrodesulfurizationof, take off virtue, diesel oil can be catalytic cracking diesel oil, coker gas oil, straight-run diesel oil etc. and their mixture.The inventive method can also be used in making with extra care of light ends such as gasoline, kerosene or VGO etc. and handle than the cracking of heavy distillat.The inventive method can be used for the gas-liquid counter current operating process in fields such as environmental improvement, chemical industry, light industry.
The catalyst of the inventive method (or filler) bed can make liquid phase under the gravity effect by catalyst granules between and/or on the catalyst granules millimetre-sized duct flow downward, and gas phase can alternately upwards flow in the millimeter grade hole road between catalyst granules and on the catalyst granules under the effect of pressure drop.This reactor has gas phase and liquid phase and is similar in different passages and flows, and mass transfer effect is preferably arranged between the gas-liquid two-phase, and high liquid speed causes pressure to fall small increase, and high gas speed causes liquid holdup that small increase is arranged.Compare with prior art, the inventive method efficiently solves the liquid flooding problem, has improved exercisable gas-liquid ratio, has increased the stability and the flexibility of operation.In addition, the inventive method is by structure, optimize the source in three grades of bed ducts, ratio and formation, particularly controlling bed voidage is made of by a certain percentage space of particle own and intergranular space, the space of particle own is compared more fixing on yardstick with the intergranular space, on distributing, compare more even, this just makes that the space of whole bed is balanced more, and balanced distribution of pores has further improved the contacting efficiency of gas-liquid counter current, gas, gas-liquid two-phase liquid distributes more even, improved gas, liquid, Gu the material Transfer effect between the three-phase has improved the efficient of physics mass transfer or chemical reaction.In addition, the inventive method adopts and huddles method loading catalyst, simple and space reactor utilization rate height.
Description of drawings
Fig. 1 is the AND DEWATERING FOR ORIFICE STRUCTURE schematic diagram that the production catalyst A is used.Specifically be of a size of: outside diameter 1.=3.0mm, leaf angle circular diameter 2.=0.50mm, the groove circular diameter 3.=0.84mm, the narrowest width of petiole 4.=0.65mm.
Fig. 2 is the AND DEWATERING FOR ORIFICE STRUCTURE schematic diagram that the production catalyst B is used.Specifically be of a size of: outside diameter 1.=3.0mm, leaf angle circular diameter 2.=0.50mm, the groove circular diameter 3.=0.72mm, the narrowest width of petiole 4.=0.33mm, 5.=40 ° angle.
The specific embodiment
Following embodiment further specifies of the present invention.
Main operating flexibility and the stability of investigating the inventive method.With the diesel raw material is example, and feedstock property sees Table-1, and this test catalyst system therefor sees Table-2.Result of the test sees Table-3, table-4.
Table-1 feedstock oil main character
| Density, kg/m 3 | 0.8824 |
| S，wt％ | 6979 |
| N，wt％ | 1014 |
| Aromatic hydrocarbons, wt% | 48.6 |
| Boiling range, ℃ | |
| IBP ～EBP | 185～373 |
Table-2 catalyst main character
| Numbering | A | B | C | D | E | F |
| Shape | Three leaf posts | Four leaf posts | Raschig ring | Spherical | Bar shaped | Clover |
| Diameter, mm | 3.0 | 3.0 | 16×16 | 1.2 | 1.9 | 2.03 |
| Length, mm | 6.0 | 6.0 | / | / | 4.5 | 6.5 |
| Voidage own | 0.38 | 0.43 | 0.49 | / | / | / |
Table-3 embodiment
| Embodiment | Catalyst | Bed voidage | The space of particle own accounts for bed space, % | | Test number | |||||||
| 1 | 2 | 3 | 4 | |||||||||
| Liquid velocity cm/s in the device | 0.350 | 0.531 | 0.708 | 0.885 | ||||||||
| 1 | A | 0.58 | 65 | The liquid flooding hydrogen-oil ratio | 2309 | 1313 | 620 | 316 | ||||
| 2 | B | 0.63 | 68 | 2453 | 1533 | 750 | 460 | |||||
| 3 | C | 0.71 | 69 | 2569 | 1798 | 879 | 623 | |||||
| 4 | A∶F＝1∶1 | 0.51 | 37 | 2142 | 1154 | 523 | 235 | |||||
| 5 | B∶E＝1∶1 | 0.53 | 41 | 2287 | 1298 | 596 | 300 | |||||
| 6 | C∶D＝1∶1 | 0.56 | 44 | 2335 | 1379 | 687 | 361 | |||||
Illustrate: wherein ratio is a volume ratio.
Table-4 comparative examples
| Comparative example | Catalyst | Bed voidage | | Test number | |||||||
| 1 | 2 | 3 | 4 | ||||||||
| Liquid velocity cm/s in the device | 0.350 | 0.531 | 0.708 | 0.885 | |||||||
| 1 | D | 0.38 | The liquid flooding hydrogen-oil ratio | 658 | 257 | 96 | 45 | ||||
| 2 | E | 0.43 | 875 | 383 | 143 | 78 | |||||
| 3 | F | 0.45 | 1211 | 494 | 226 | 119 | |||||
By table-3 with show-4 experimental result as seen, of the present invention huddle filling 3 D pore canal beds in certain device under the liquid speed hydrogen-oil ratio opereating specification be far longer than the filling scheme that huddles of existing conventional catalyst, increased the flexibility and the stability of counter-current operation device.(illustrate: the exercisable maximum hydrogen to oil volume ratio of liquid flooding for not taking place in the liquid flooding hydrogen-oil ratio, and it is wide more that the big more explanation of this value can be adjusted the operating space)
Embodiment 7～8, comparative example 4
Mainly investigate under same reaction conditions, the inventive method has promotion to reactivity worth.With the diesel raw material is example, and feedstock property sees Table-1, and this test catalyst system therefor, experimental result see Table-5.Reaction condition is: 360 ℃ of reaction temperatures, and reaction pressure 6.0MPa, volume space velocity is 1.0h during liquid
-1(with respect to the dischargeable capacity of reactor), hydrogen to oil volume ratio are 300.The catalyst of comparative example 4 is F, adopts the TLP type of reactor.
Table-5 embodiment and comparative example reactivity worth are relatively
| Experimental example | Embodiment 7 | Embodiment 8 | Comparative example 4 | |
| Catalyst property | Numbering | A | B | F |
| Carrier | Gama-alumina | |||
| Catalytic active component | Mo, W, Ni (atomic ratio 1: 1: 0.2) | |||
| Metal oxide, wt% | 29 | |||
| The reactor bed voidage | 0.58 | 0.63 | 0.60 | |
| Product | Sulfur content, μ g/g | 14 | 19 | 89 |
| Arene content, wt% | 18.2 | 18.6 | 29 | |
By data in the table as seen, under same reaction conditions, the inventive method to the deep desulfuration of diesel oil, take off arylation reaction and obvious facilitation arranged than existing counter-current process.
Claims (6)
1, a kind of method of operating of fixed bed gas-liquid counter current reactor, be included on the catalyst, gas phase and liquid phase reverse flow, the gas, liquid, solid three-phase contacts with each other material Transfer or chemical reaction takes place, it is characterized in that the employing of catalyst or filler huddles mode and loads, the voidage of bed is 0.45～0.85, catalyst adopts one or more, wherein have at least a kind of catalyst granules to have the high voidage configuration, voidage with high voidage configuration particle itself is 0.10～0.95, and the space of particle own accounts for 10～90% of bed space; Wherein said gas phase is a hydrogen, and described liquid phase is a diesel oil, and described beds is the catalyst for hydrogenation treatment of diesel oil bed; Described beds has three grades of ducts: the catalyst particles intragranular has nanoscale and/or micron order duct, and the catalyst particles intergranular has millimeter grade hole road or space, and catalyst granules originally has millimetre-sized duct or groove on one's body; Process conditions are: 200～427 ℃ of reaction temperatures; Reaction pressure is 1.0～20.0MPa; Hydrogen to oil volume ratio is 50～1000; Volume space velocity is 0.1-10.0h during liquid
-1
2, in accordance with the method for claim 1, it is characterized in that described beds uses the catalyst of high voidage configuration to huddle filling and constitutes; Or, huddle filling after the mixing and constitute the catalyst and the high voidage configuration catalyst of conventional configuration.
3, in accordance with the method for claim 1, it is characterized in that described high voidage configuration catalyst is meant particle outer surface or inner shape of catalyst with millimeter grade hole road or groove.
4, in accordance with the method for claim 3, it is characterized in that described high voidage configuration catalyst is two leaf posts, three leaf posts, four leaf posts, annular, Raschig ring, butterfly or road with holes sphere.
5, in accordance with the method for claim 1, it is characterized in that the space of described catalyst for hydrogenation treatment of diesel oil particle own accounts for 30～80% of bed space.
6, in accordance with the method for claim 1, the process conditions that it is characterized in that the diesel oil countercurrent hydrogenation are: 200～380 ℃ of reaction temperatures; Reaction pressure is 3.0～12.0MPa; Hydrogen to oil volume ratio is 50～500; Volume space velocity is 0.5-7.5h during liquid
-1
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 03133565 CN1251794C (en) | 2003-05-31 | 2003-05-31 | Operating method for fixed bed gas-liquid counter current reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 03133565 CN1251794C (en) | 2003-05-31 | 2003-05-31 | Operating method for fixed bed gas-liquid counter current reactor |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1552511A CN1552511A (en) | 2004-12-08 |
| CN1251794C true CN1251794C (en) | 2006-04-19 |
Family
ID=34323103
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 03133565 Expired - Lifetime CN1251794C (en) | 2003-05-31 | 2003-05-31 | Operating method for fixed bed gas-liquid counter current reactor |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1251794C (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101870665B (en) * | 2010-05-18 | 2014-04-30 | 中国科学院过程工程研究所 | Gas-liquid-solid three-phase counter-current reaction device and method for pyrolytic reaction of carbamic acid ester |
| CN109506495B (en) * | 2018-12-19 | 2024-03-19 | 中冶焦耐(大连)工程技术有限公司 | Quadrangle loose material layer filler |
| CN114540078A (en) * | 2020-11-24 | 2022-05-27 | 何巨堂 | Simulated deposition filtration method for hydrocarbon raw material in fixed bed hydrogenation reaction process |
-
2003
- 2003-05-31 CN CN 03133565 patent/CN1251794C/en not_active Expired - Lifetime
Also Published As
| Publication number | Publication date |
|---|---|
| CN1552511A (en) | 2004-12-08 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US8329028B2 (en) | Solid catalyst hydrocarbon conversion process using stacked moving bed reactors | |
| CN101942333B (en) | Shale oil single-stage serial hydrocracking technology method | |
| JP4469601B2 (en) | Molded trilobal particles | |
| JP2009520060A (en) | Reactor for reforming heavy oil mixed with slurry-like highly active catalyst composition | |
| CN1537155A (en) | Hydrotreating process and catalyst | |
| AU2002331370A1 (en) | Shaped trilobal particles | |
| CN101942317B (en) | Method for grading fluidized bed catalysts | |
| JP2005509083A (en) | Countercurrent hydrotreatment | |
| CN1251794C (en) | Operating method for fixed bed gas-liquid counter current reactor | |
| WO2002079128A1 (en) | Mini-structured catalyst beds for three-phase chemical processing | |
| CN102041081A (en) | Combined method of hydrocracking and producing lubricant oil base oil | |
| US6325919B1 (en) | Catalyst support, catalyst, reactor for hydrogenation reaction, and catalytic reaction method | |
| US20210322943A1 (en) | Resaturation of gas into a liquid feedstream | |
| CN104927910B (en) | A kind of diesel oil hydro-upgrading method and a kind of hydrogenation reaction device | |
| CN102041069A (en) | Gas-liquid countercurrent hydrogenation method for desulfurization, denitrification and aromatic hydrocarbon of diesel | |
| JP6395709B2 (en) | Hydrocarbon oil hydrotreating method | |
| CN103666545B (en) | A kind of diesel oil hydrofining method | |
| CN1277906C (en) | Diesel oil hydrotreating method | |
| US7435336B2 (en) | Process for carrying out gas-liquid countercurrent processing | |
| Sie et al. | Monolithic reactor for countercurrent gas-liquid operation | |
| CN102465013B (en) | A kind of high virtue is containing diesel oil hydro-upgrading method | |
| WO2006065127A1 (en) | Multiphase reactions using solid foams | |
| CN1212181C (en) | Gas-liquid counter current processing and treating method | |
| Stemmet et al. | Multiphase reactions using solid foams | |
| JP2007270067A (en) | Method for hydrocracking wax and method for producing fuel base |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CX01 | Expiry of patent term | ||
| CX01 | Expiry of patent term |
Granted publication date: 20060419 |