CN1060405C - Catalysis-distillation equipment by mixing erecting catalyst with fraction elements - Google Patents
Catalysis-distillation equipment by mixing erecting catalyst with fraction elements Download PDFInfo
- Publication number
- CN1060405C CN1060405C CN97106049A CN97106049A CN1060405C CN 1060405 C CN1060405 C CN 1060405C CN 97106049 A CN97106049 A CN 97106049A CN 97106049 A CN97106049 A CN 97106049A CN 1060405 C CN1060405 C CN 1060405C
- Authority
- CN
- China
- Prior art keywords
- catalyst
- fraction elements
- catalysis
- fraction
- elements
- 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 - Fee Related
Links
- 239000003054 catalyst Substances 0.000 title claims abstract description 61
- 238000004821 distillation Methods 0.000 title claims abstract description 27
- 239000000463 material Substances 0.000 claims description 21
- 229910000831 Steel Inorganic materials 0.000 claims description 16
- 239000010959 steel Substances 0.000 claims description 16
- 238000005194 fractionation Methods 0.000 claims description 15
- 239000000945 filler Substances 0.000 claims description 14
- 238000012946 outsourcing Methods 0.000 claims description 14
- 238000011068 loading method Methods 0.000 claims description 9
- 238000012856 packing Methods 0.000 claims description 9
- 229910001220 stainless steel Inorganic materials 0.000 claims description 5
- 239000010935 stainless steel Substances 0.000 claims description 5
- 238000011049 filling Methods 0.000 claims description 4
- RGCLLPNLLBQHPF-HJWRWDBZSA-N phosphamidon Chemical group CCN(CC)C(=O)C(\Cl)=C(/C)OP(=O)(OC)OC RGCLLPNLLBQHPF-HJWRWDBZSA-N 0.000 claims description 3
- 230000001413 cellular effect Effects 0.000 claims description 2
- 238000006243 chemical reaction Methods 0.000 abstract description 61
- 230000003197 catalytic effect Effects 0.000 abstract description 7
- 238000004519 manufacturing process Methods 0.000 abstract description 4
- 239000000376 reactant Substances 0.000 abstract description 4
- 150000001993 dienes Chemical class 0.000 description 11
- 239000007791 liquid phase Substances 0.000 description 9
- 238000005984 hydrogenation reaction Methods 0.000 description 8
- 239000000203 mixture Substances 0.000 description 8
- 239000002994 raw material Substances 0.000 description 8
- 239000012808 vapor phase Substances 0.000 description 7
- VQTUBCCKSQIDNK-UHFFFAOYSA-N Isobutene Chemical compound CC(C)=C VQTUBCCKSQIDNK-UHFFFAOYSA-N 0.000 description 6
- 150000001336 alkenes Chemical group 0.000 description 5
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 4
- BZLVMXJERCGZMT-UHFFFAOYSA-N Methyl tert-butyl ether Chemical compound COC(C)(C)C BZLVMXJERCGZMT-UHFFFAOYSA-N 0.000 description 4
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 4
- 229910052593 corundum Inorganic materials 0.000 description 4
- 239000001257 hydrogen Substances 0.000 description 4
- 229910052739 hydrogen Inorganic materials 0.000 description 4
- 238000000034 method Methods 0.000 description 4
- 238000012360 testing method Methods 0.000 description 4
- 229910001845 yogo sapphire Inorganic materials 0.000 description 4
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 241000313287 Oncopera intricata Species 0.000 description 3
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 description 3
- 239000002253 acid Substances 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 3
- 238000010992 reflux Methods 0.000 description 3
- MYRTYDVEIRVNKP-UHFFFAOYSA-N 1,2-Divinylbenzene Chemical compound C=CC1=CC=CC=C1C=C MYRTYDVEIRVNKP-UHFFFAOYSA-N 0.000 description 2
- VXNZUUAINFGPBY-UHFFFAOYSA-N 1-Butene Chemical compound CCC=C VXNZUUAINFGPBY-UHFFFAOYSA-N 0.000 description 2
- 241000282326 Felis catus Species 0.000 description 2
- PPBRXRYQALVLMV-UHFFFAOYSA-N Styrene Chemical compound C=CC1=CC=CC=C1 PPBRXRYQALVLMV-UHFFFAOYSA-N 0.000 description 2
- 241000219793 Trifolium Species 0.000 description 2
- 239000012752 auxiliary agent Substances 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 230000032050 esterification Effects 0.000 description 2
- 238000005886 esterification reaction Methods 0.000 description 2
- 238000006266 etherification reaction Methods 0.000 description 2
- 239000004744 fabric Substances 0.000 description 2
- 239000011347 resin Substances 0.000 description 2
- 229920005989 resin Polymers 0.000 description 2
- 238000009834 vaporization Methods 0.000 description 2
- 230000008016 vaporization Effects 0.000 description 2
- YHQXBTXEYZIYOV-UHFFFAOYSA-N 3-methylbut-1-ene Chemical compound CC(C)C=C YHQXBTXEYZIYOV-UHFFFAOYSA-N 0.000 description 1
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 1
- 229910003296 Ni-Mo Inorganic materials 0.000 description 1
- 229910002666 PdCl2 Inorganic materials 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 150000001335 aliphatic alkanes Chemical class 0.000 description 1
- 150000001345 alkine derivatives Chemical class 0.000 description 1
- 230000029936 alkylation Effects 0.000 description 1
- 238000005804 alkylation reaction Methods 0.000 description 1
- XFBXDGLHUSUNMG-UHFFFAOYSA-N alumane;hydrate Chemical compound O.[AlH3] XFBXDGLHUSUNMG-UHFFFAOYSA-N 0.000 description 1
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 1
- 125000003118 aryl group Chemical group 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 238000004523 catalytic cracking Methods 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 235000019628 coolness Nutrition 0.000 description 1
- 238000007334 copolymerization reaction Methods 0.000 description 1
- 230000009849 deactivation Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000011491 glass wool Substances 0.000 description 1
- 239000008187 granular material Substances 0.000 description 1
- 238000005470 impregnation Methods 0.000 description 1
- 238000006317 isomerization reaction Methods 0.000 description 1
- 239000011344 liquid material Substances 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 229910044991 metal oxide Inorganic materials 0.000 description 1
- 150000004706 metal oxides Chemical class 0.000 description 1
- 229910052976 metal sulfide Inorganic materials 0.000 description 1
- 239000002808 molecular sieve Substances 0.000 description 1
- DDTIGTPWGISMKL-UHFFFAOYSA-N molybdenum nickel Chemical compound [Ni].[Mo] DDTIGTPWGISMKL-UHFFFAOYSA-N 0.000 description 1
- 150000007524 organic acids Chemical class 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 229910052763 palladium Inorganic materials 0.000 description 1
- PIBWKRNGBLPSSY-UHFFFAOYSA-L palladium(II) chloride Chemical compound Cl[Pd]Cl PIBWKRNGBLPSSY-UHFFFAOYSA-L 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 239000004033 plastic Substances 0.000 description 1
- 229910052573 porcelain Inorganic materials 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 1
- 239000011973 solid acid Substances 0.000 description 1
- 238000004230 steam cracking Methods 0.000 description 1
- 238000006277 sulfonation reaction Methods 0.000 description 1
Images
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The present invention relates to a catalytic distillation device. A reaction section is formed by the combination of purpose-made fractionating elements, reactants generate reaction under the function of a catalyst and simultaneously carry out a fractionating function on the surfaces of the fractionating elements until the reaction is completed or reaches a certain requirement. The present invention has the advantages of simple structure of the reaction section, low manufacturing cost, convenient operation and high reaction efficiency.
Description
The present invention relates to a kind of catalysis-distillation equipment.
Catalytic distillation technology is that reaction is separated in the same catalysis-distillation equipment and carries out with product, when reaction is carried out the product that generates is separated, and the balance of reaction is broken, thereby makes the reaction trend fully, improves the conversion ratio of reactant; Reaction heat can be absorbed by the vaporization of reaction mass in addition, thereby not only reaction temperature can keep constant, and energy consumption can greatly reduce, and technological process is simplified, and investment also greatly reduces.Catalytic distillation tower is generally formed by three sections: top is rectifying section, and the middle part is a catalyst reaction section, and the bottom is a stripping section.In this catalytic distillation tower, the liquid phase material that flows downward must also react and the product fractionation by the middle part catalyst reaction section therein simultaneously with the vapor-phase material that upwards flows in convection current, yet general catalyst grain size is smaller, the resistance of beds convection cell is big, make vapor-phase material that upwards flows and the liquid phase material that flows downward be difficult to convection current by the middle part conversion zone, thereby making it can't normal running, reaction can't be carried out with fractionation.
Many conversion zone special constructions have been developed for addressing the above problem reported in literature, as US.3,434, the 534th, catalyst is seated in the downspout of middle part conversion zone plate and reacts as setting up reactor, fractionation is carried out on tower tray, the loadings of this method catalyst is restricted, and catalyst loads also more complicated.US.4,439, a kind of structure of 350 inventions is contained in catalyst in the catalyst corbie, many this corbies are installed on the separation tray of middle part conversion zone, liquid phase reacting material is flowed through tower tray when carrying out fractionation, diffuses in the catalyst corbie and reacts, and the number of the little small basket of the catalyst of the required installing of this structure is a lot, install also very complicated, the cost height.US.4,215,011 has invented a kind of catalyst packing method, the fine granularity catalyst is contained in one to be arranged in the stripe shape pouch made from the glass wool cloth sheet, and the laying last layer can strut the stainless steel cloth in space, being rolled into helical coil then is seated in the conversion zone, there is free space can make liquid phase material and vapor-phase material convection current in the helical coil by the middle part conversion zone, reactant diffuses in the pouch to contact with catalyst and reacts, this structure manufacturing, filling complexity, reactant must diffuse in the bag and just can react, and influences reaction efficiency.US.5,057,468 discloses the catalytic distillation technology that a kind of catalyst and fraction elements load in mixture, its used fraction elements is a hollow, the fraction elements surface is little, thereby fractionating effect is poor, fraction elements also will add the lid at two ends, make make complicated.
The shortcoming of above-mentioned these structures and other similar structures is a complex structure, the manufacturing expense height, and the workman need enter in the tower and operate during the loading and unloading catalyst, and operating difficulties, reaction efficiency are also not high.
The catalysis-distillation equipment that the objective of the invention is to overcome the deficiencies in the prior art and provide a kind of catalyst and fraction elements to load in mixture, the fraction elements area is big, and the reaction efficiency height is simple in structure, makes easily.
Catalysis-distillation equipment of the present invention, be that conversion zone is improved, mixed packing catalyst and fraction elements on the support orifice plate of reacting section catalyst bed, the major technique characteristics are that catalyst is between each fraction elements, fraction elements is by side-wall hole, and the element of outsourcing steel wire constitutes.
Above-mentioned fraction elements can also be on the basis of said elements in filling can increase the material of fraction elements area.
The material of loading in the fraction elements preferably has netted or cellular, undulatory material.Fraction elements of the present invention comprises that also conventional fractionation filler adds the form of steel wire.Increased the surface area of conventional fractionation filler.
Catalyst of the present invention and fraction elements load in mixture, and fraction elements has bigger surface, thereby improve fractionation and reaction efficiency.The eyelet size of outer steel silk screen will be easy to make vapour, liquid material to pass, and catalyst granules is passed, the filling of catalyst and the fraction elements when size of fraction elements is wanted and can be formed enough free spaces at conversion zone, so that upwards the vapor-phase material that flows passes through beds with the liquid phase material convection current that flows downward, and it is fully contacted with catalyst and fraction elements, react and fractionation.
The volume ratio of fraction elements and catalyst is: 10～90: 90～10, be preferably 40～60: and 60～40, the equivalent diameter of fraction elements is 5～60mm, is preferably 10～25mm.The shape of fraction elements can be a helical form fractionation filler.Also can be by side-wall hole, interior dress ripple packing, the column type that outsourcing steel wire (15) constitutes; By side-wall hole, interior dress stainless steel Dixon ring filler, the column type that the outsourcing steel wire constitutes; By inwall the filler of strip tongue type opening is arranged, the column type that the outsourcing steel wire constitutes.And the fraction elements with big surface of analogous shape.The ratio of height to diameter of above-mentioned these cylindrical fraction elements preferably 0.5～3: 1 is preferably than being 1: 1～1.5: 1.Fraction elements can form with steel, porcelain, plastic production.Catalyst can be strip, spherical or other shapes.
Fig. 1 is the structural representation of catalysis-distillation equipment, and this equipment 1 is by upper rectifying section 2, middle part conversion zone 3, and bottom stripping section 4 is formed.Conversion zone is made up of several beds, and the bed bottom is a porous catalyst gripper shoe 5, and its perforate size wants to make liquid phase that flows downward and the vapour phase that upwards flows to pass through, and catalyst 7 and fraction elements 6 are spilt.Loading catalyst 7 and fraction elements 6 on the gripper shoe 5.Upper rectifying section and bottom stripping section can use conventional plate or fractionation filler, and catalyst and fraction elements loading port 8 can be established in each bed top, the bottom is established and unloaded outlet 9 in order to loading and unloading catalyst and fraction elements.Can draw off catalyst with fraction elements behind the catalysqt deactivation, the fraction elements behind the sieve de-inactivation catalyst can mix with raw catelyst and reloads.Be added in the tower between top, bottom or the bed of needs by the conversion zone of tower of raw material 12 according to raw material properties and reaction, flow downward by the beds of middle part conversion zone from the liquid phase material of rectifying section orlop tower tray; From stripping section topmost the vapor-phase material of tower tray then upwards flow through the beds of conversion zone, liquid phase material and vapor-phase material react and fractionation on bed simultaneously, reach to react completely or meet the requirements of till the conversion ratio.The vapor-phase material that upwards flows in the reaction back is come out after condenser 10 coolings by cat head, and a part is returned the catalytic distillation cat head as backflow, and a part goes out device as low boiling product 13; The liquid phase material that flows downward after the reaction goes out device at the bottom of by tower, and a part is at the bottom of returning tower after reboiler 11 vaporizations, and a part goes out device as product 14.The overhead product quality is not being required or when less demanding, also can not establish rectifying section.The catalyst loading amount is calculated according to the requirement of material feeding amount, composition and conversion ratio and is determined in the conversion zone, and the several amounts according to catalyst of bed are determined.The quantity of fraction elements need be enough to product separated so that react and carry out fully.
Fig. 2, Fig. 6 are the fraction elements of shape fractionation filler in the shape of a spiral, and Fig. 6 is the vertical view of Fig. 2;
Fig. 3, Fig. 7 are by side-wall hole (17), interior dress ripple packing (18), and the fraction elements of the column type (16) that outsourcing steel wire (15) constitutes, Fig. 7 is the vertical view of Fig. 3;
Fig. 4, Fig. 8 are by side-wall hole (17), interior dress stainless steel Dixon ring filler (19), and the fraction elements of the column type (16) that the outsourcing steel wire constitutes, Fig. 8 is the vertical view of Fig. 4;
Fig. 5, Fig. 9 are by side-wall hole (17), and inwall has the filler (20) of strip tongue type opening, the fraction elements of the column type (16) that the outsourcing steel wire constitutes, and Fig. 9 is the vertical view of Fig. 5.
Catalyst of the present invention can be the acidic catalyst for reactions such as etherificate, esterification, alkylations, also can be carrier model metal, metal oxide, the metal sulfide catalyst for hydrogenation reaction or the corresponding catalyst that is used for other reactions. As carrying out etherification reaction pure and tertiary olefin, the acid catalyzed reactions such as alcohol and organic acid esterification can use azochlorosulfonate acid resin catalyst; The alkylated reaction of alkene and alkane, aromatic hydrocarbons and alkene can use molecular sieve catalyst, solid acid catalyst; Carry out to use the Pd-Al2O3 catalyst when hydrocarbon-fraction selects hydrogenation to take off diolefin, alkynes, can use Ni-Al2O3 or Pt-Al2O3 catalyst when aromatic hydrogenation is saturated, can use Ni-Mo/Ni-W-Al2O3 catalyst etc. during hydrofinishing. The shape of catalyst can be spherical, bar shaped or clover bar shaped.
Advantage of the present invention: simple in structure, loading and unloading catalyst processing ease, fraction elements has larger area, and it is slightly large that the hole of sidewall can be opened, and two ends must be not with cover, makes easily, and reaction efficiency is high.
Embodiment 1:
Add auxiliary agent with aluminium hydrate powder and be squeezed into φ 1.5 * 3～15mm trifolium-shaped carrier, making it contain the palladium amount with the PdCl2 solution impregnation after the roasting is 0.3～0.35%, with being used for C3, C4, C 5 fraction selection hydrogenation and removing diolefin catalyst behind the hydrogen reducing.
Carry out the steam cracking C 4 fraction with catalysis-distillation equipment of the present invention and select the reaction of hydrogenation and removing diolefin, catalyst and screw type fractionation filler loaded in mixture at conversion zone in 1: 1 by volume.Result of the test is as follows:
| The project indicator |
| Diolefin content %m/m 1.0 reaction volume air speed h in the C4 raw material -1Diolefin content ppm＜20 among the C4 behind butene-1 yield (selectively) %m/m 98.49 hydrogenation behind ratio mol/mol 1.5 conversion zone temperature ℃ 40～60 reaction pressure MPa, 0.5 volume reflux ratio, 1.0 hydrogenation of 20 hydrogen and diolefin |
Embodiment 2:
With styrene and divinylbenzene and auxiliary agent copolymerization balling-up, dry then sulfonation glomeration high activity azochlorosulfonate acid resin catalyst, be used for the isobutene of C 4 fraction and the reaction that the methyl alcohol reaction generates MTBE (methyl tertiary butyl ether(MTBE)).Result of the test is as follows:
Use catalysis-distillation equipment of the present invention, catalyst and opening of external wall, the fraction elements of interior dress ripple packing by volume: load in mixture at conversion zone at 1: 1.2.Result of the test is as follows:
| The project indicator |
| Isobutene content %m/m 21.91 reaction volume air speed h in the raw material -13 operating pressure MPa, 0.75 alfin ratio mol/mol, 1.1 conversion zone temperature ℃ 60～70 volume reflux ratios, 1.0 isobutene conversion %m/m, 99.49 MTBE %m/m 99.10 |
Embodiment 3:
With embodiment 1 Pd/A12O3 clover bar shaped catalyst of making and the fraction elements of forming by φ 30 * 30mm strip tongue type opening outsourcing 40 order stainless steel cloths, by the reaction distillation section of 0.5: 1 volume ratio mixed packing, be used for the selection hydrogenation of catalytic cracking C 5 fraction alkadienes at catalytic distillation tower.100～130 ℃ of the temperature of control reaction distillation section, reaction pressure 1.0MPa, the mol ratio of hydrogen and alkadienes is 1.5～10 o'clock, the 8000PPM of diene content from raw material among the C5 dropped to less than 100PPM, but but the yield of etherificate tertiary olefin reach more than 65% greater than the isomerization rate that the 3-methyl-1-butene isomery of 104% no etherification reaction activity turns to the etherificate component, produce gasoline and contain the quality raw materials that oxygen adds component TAME thereby can be used as.Result of the test is as follows:
| The project indicator |
| Diolefin content %m/m 0.86 reaction volume air speed h in the raw material -1But 3.0 diolefin content ppm＜100 in the raw material after tertiary olefin yield (selectively) %m/m of hydrogen and ratio mol/mol 6.0 conversion zone mean temperatures ℃ 110～120 reaction pressure Mpa, 1.0 volume reflux ratios, 1.0 etherificates of diolefin＞104 reactions |
Claims (9)
1, a kind of catalysis-distillation equipment, mixed packing catalyst and fraction elements on the support orifice plate of reacting section catalyst bed is characterized in that catalyst between each fraction elements, and fraction elements is by side-wall hole, and the element of outsourcing steel wire constitutes.
2, catalysis-distillation equipment according to claim 1 is characterized in that fraction elements is by side-wall hole, the outsourcing steel wire, and the material that interior filling can increase the fraction elements area constitutes.
3, catalysis-distillation equipment according to claim 2 is characterized in that loading in the fraction elements and has netted or cellular, undulatory material.
4,, it is characterized in that fraction elements can be any in the following shape according to claim 1 or 2 or 3 described catalysis-distillation equipments:
(1) helical form fractionation filler;
(2) side-wall hole, interior dress ripple packing, the column type that the outsourcing steel wire constitutes;
(3) side-wall hole, interior dress stainless steel Dixon ring filler, the column type that the outsourcing steel wire constitutes;
(4) inwall has strip tongue type opening filler, the column type that the outsourcing steel wire constitutes.
5, catalysis-distillation equipment according to claim 4 is characterized in that the ratio of height to diameter of column type is: 0.5～3: 1.
6, catalysis-distillation equipment according to claim 5 is characterized in that ratio of height to diameter the best of column type is: 1: 1～1.5: 1.
7, a kind of catalysis-distillation equipment, mixed packing catalyst and fraction elements on the support orifice plate of reacting section catalyst bed is characterized in that catalyst between each fraction elements, fraction elements is to be made of conventional fractionation filler outsourcing steel wire.
8, according to claim 1 or 2 or 7 described catalysis-distillation equipments, the equivalent diameter that it is characterized in that fraction elements is 5～60mm, and the best is 10～25mm.
9,, it is characterized in that the volume ratio of fraction elements and catalyst is according to claim 1 or 2 or 7 described catalysis-distillation equipments: 10～90: 90～10, the best is 40～60: 60～40.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN97106049A CN1060405C (en) | 1997-08-20 | 1997-08-20 | Catalysis-distillation equipment by mixing erecting catalyst with fraction elements |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN97106049A CN1060405C (en) | 1997-08-20 | 1997-08-20 | Catalysis-distillation equipment by mixing erecting catalyst with fraction elements |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1208663A CN1208663A (en) | 1999-02-24 |
| CN1060405C true CN1060405C (en) | 2001-01-10 |
Family
ID=5168326
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN97106049A Expired - Fee Related CN1060405C (en) | 1997-08-20 | 1997-08-20 | Catalysis-distillation equipment by mixing erecting catalyst with fraction elements |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1060405C (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104771924B (en) * | 2015-04-15 | 2016-06-08 | 中国科学院广州能源研究所 | A device and method for preparing furfural coupled with ethanol rectification |
| CN107345148A (en) * | 2017-07-07 | 2017-11-14 | 鄂尔多斯市易臻石化科技有限公司 | C4The method and apparatus that cut synthesizes high octane gasoline component with formaldehyde |
| CN115571969B (en) * | 2022-11-10 | 2023-06-13 | 华夏碧水环保科技股份有限公司 | Fenton reactor |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US447154A (en) * | 1891-02-24 | Car-coupling | ||
| US4471154A (en) * | 1983-06-10 | 1984-09-11 | Chevron Research Company | Staged, fluidized-bed distillation-reactor and a process for using such reactor |
| US5057468A (en) * | 1990-05-21 | 1991-10-15 | Chemical Research & Licensing Company | Catalytic distillation structure |
-
1997
- 1997-08-20 CN CN97106049A patent/CN1060405C/en not_active Expired - Fee Related
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US447154A (en) * | 1891-02-24 | Car-coupling | ||
| US4471154A (en) * | 1983-06-10 | 1984-09-11 | Chevron Research Company | Staged, fluidized-bed distillation-reactor and a process for using such reactor |
| US5057468A (en) * | 1990-05-21 | 1991-10-15 | Chemical Research & Licensing Company | Catalytic distillation structure |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1208663A (en) | 1999-02-24 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US4847430A (en) | Process for manufacturing a tertiary alkyl ether by reactive distillation | |
| CN1063352C (en) | Multi-purpose catalytic distillation column and etherification process using same | |
| US5026459A (en) | Apparatus for reactive distillation | |
| KR100457472B1 (en) | Apparatus comprising a catalyst distillation zone with a reaction zone in which hydrogen is distributed | |
| US4439350A (en) | Contact structure for use in catalytic distillation | |
| KR100787690B1 (en) | Hydrogenation of Benzene to Cyclohexane | |
| CN105367368B (en) | The method that high-purity isobutylene is prepared from C_4 hydrocarbon | |
| JPH10168465A (en) | Method for hydrogen-reducing and isomerizing petroleum product containing benzene | |
| US5523061A (en) | Equipment for catalytic distillation | |
| CN1060405C (en) | Catalysis-distillation equipment by mixing erecting catalyst with fraction elements | |
| CA2604486A1 (en) | Double bond hydroisomerization process | |
| CN1020411C (en) | Mixed phase catalysis reaction distillation technology and equipment | |
| CN101391150A (en) | A catalytic distillation tower reaction section structure | |
| CN1345617A (en) | Catalytic reaction distillation equipment | |
| Yang et al. | Efficient Cu-based catalysts for the selective demethoxylation of guaiacols | |
| CN102516036A (en) | Process method for preparing methyl tert-butyl ether by differential reaction rectification and equipment for same | |
| WO2006124167A2 (en) | Improved double bond hydroisomerization process | |
| CN116059926B (en) | Hydrofractionation reactor and combined reactor | |
| US7977391B2 (en) | Process for producing condensed-phase product from one or more gas-phase reactants | |
| CN1429656A (en) | Catalytic distillation tower structure | |
| CN101306256B (en) | Catalyst distillation column internals for high effective mass transfer | |
| CN104511312A (en) | Catalyst used for catalytic rectification selective hydrogenation, preparation method and application thereof | |
| CN1071443A (en) | A kind of catalyzer that is used for one-stage selective hydrogenation of gasoline splitting | |
| CN1074680C (en) | Shell and tube type catalytic distillation equipment | |
| GB2078745A (en) | Production of alcohols from synthesis gas |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C06 | Publication | ||
| PB01 | Publication | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C19 | Lapse of patent right due to non-payment of the annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |