CN1242249A - Shell and tube type catalytic distillation equipment - Google Patents
Shell and tube type catalytic distillation equipment Download PDFInfo
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- CN1242249A CN1242249A CN 98110352 CN98110352A CN1242249A CN 1242249 A CN1242249 A CN 1242249A CN 98110352 CN98110352 CN 98110352 CN 98110352 A CN98110352 A CN 98110352A CN 1242249 A CN1242249 A CN 1242249A
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- fractionating column
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- distillation equipment
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Abstract
This invention catalytic distillation equipment is characterized by that the tower body includes rectification section, reaction section and gas stripping section; the reaction section is composed of vertically arranged fractionating tubes and there are catalyst between the fractionating tubes. The fractionating tube wall has holes, the outside of fractionating tube has steel wire mesh or a layer of mesh is lined inside the tube. The fractionating tubes are fixed on the inside of tower body with a fixing plate for fixing the two ends of the fractionating tube. The present invention is simple in structure, large in catalyst loading quantity, easy to install and handle, and can effectively proceed reaction and fractionating of product with high reaction rate.
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 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 (not high to the quality requirement of overhead product or can not establish rectifying section when not requiring) middle part is catalyst reaction section, and the bottom is a stripping section.In 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 normally be carried out with fractionation.
Be many conversion zone special constructions that addressed the above problem reported in literature, as USP.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.USP.4,471, a kind of structure of 154 inventions be catalyst be contained in the made fluid made by fabric or stainless steel cloth by but do not make in the catalyst parcel that catalyst passes through, again these parcels are placed on the plate of middle part conversion zone, be diffused into when making reactant flow through plate and contact with catalyst in the parcel and react, the catalyst loading amount of this structure also is restricted.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 also must diffuse in the bag and just can react, and influences reaction efficiency.
The shortcoming of above-mentioned these structures and other similar structures is a complex structure, the manufacturing expense height, and reaction efficiency is low.
The purpose of this invention is to provide a kind of shell and tube type catalytic distillation equipment, reaction segment structure is simple, and loaded catalyst is big, and loading and unloading are easy, and catalytic reaction and fractionating efficiency height improve the conversion ratio of reaction.
Shell and tube type catalytic distillation equipment, its major technique characteristics are that conversion zone is made up of the catalyst between fractionating column that is fixed in the vertical arrangement in the tower body and fractionating column.
The tube wall of above-mentioned fractionating column has mouth, tube wall outsourcing steel wire or pipe liner one deck net.The mesh size of steel wire or net can make gas and liquid by but catalyst is passed through.Fractionating column can be circle, rectangle or other shape, and the tube wall opening can be hole, strip ligulate opening etc.In order to improve fractionating efficiency, can be filled with the fractionation filler in the fractionating column.This fractionation filler can adopt conventional fillers.
Fractionating column is that the fixed head by two ends is fixed in the tower body, between the fractionating column of upper mounted plate perforate is arranged.Liquid phase material can enter beds by this perforate.Bottom plate also is the gripper shoe of catalyst.
The diameter of circular fractionating column is 10～200mm, 30～80mm preferably, and the width of rectangle fractionating column is 10～200mm, 30～80mm preferably, the distance between the fractionating column is 5～100mm, is preferably 20～50mm.
Catalytic distillation tower, the top in the tower body is rectifying section, and the middle part is a conversion zone, and the bottom is a stripping section, not high to the quality requirement of overhead product or can not establish rectifying section when not requiring.
The loadings of catalyst requires decision according to reaction conversion ratio, and then according to the decision of catalyst total filling amount height, conversion zone bed number generally is divided into 1～10 to the bed hop count, is preferably 3～6.The catalyst loading port is established on each bed top, and the bottom is established catalyst and unloaded outlet, in order to the loading and unloading catalyst, also has needed import and export such as raw material, product on the tower body.
Below in conjunction with the embodiment description of drawings:
Fig. 1 is the structural representation of catalytic distillation tower;
Fig. 2～Fig. 4 is the structural representation of fractionating column;
Fig. 5 is the A-A view.
Among the figure: 1 tower body, 2 rectifying sections, 3 conversion zones, 4 stripping sections, 5 steel wires, 6 beds, 7 fractionating columns, 8 catalyst loading ports, 9 catalyst unload outlet 10 upper mounted plates 11 fractionating column tube wall openings 12 upper mounted plate perforates 13 bottom plates 14 condensers 15 reboilers
Such as Fig. 2～4, fractionating column 7 can be circular, also can be rectangle, and tube wall has opening 11, and opening can be the hole, also can be strip ligulate opening. Tube wall is surrounded by layer of steel wire net 5 outward and is fixedly connected with fractionating column. Each bed of tower body 1 internal reaction section 3, with the tower wall fractionating column 7 that is arranged in parallel, the fractionating column both ends open is fixed in the tower body by upper mounted plate 10 and bottom plate 13, and bottom plate also is the gripper shoe of catalyst. Perforate 12 is arranged between fractionating column on the upper mounted plate. It is beds 6 between fractionating column. Rectifying section 2 and stripping section 4 can use conventional plate or fractionation filler.
Directly enter beds 6 from the liquid phase material part of rectifying section 2 bottoms via perforate 12 between the pipe of upper mounted plate 10 and react, and lateral flow is diffused in the fractionating column 7; Another part enters fractionating column by the fractionating column open top and flows downward, and enters fractionating column and carries out fractionation with the liquid phase material convection current that flows downward by fractionating column with the vapor-phase material that upwards flows from stripping section top or next bed. Vapour in the fractionating column, liquid phase material diffuse into beds 6 by the hole on the fractionating column tube wall and steel wire 5 and contact with catalyst and react, and reacted product diffuses out and enters fractionating column and carry out the product fractionation. Flow to its next reaction bed top from a upper reacted liquid phase material of bed by its bottom, carry out same as mentioned above reaction and fractionation, carry out reagentia at beds, carry out the fractionation of product in fractionating column and the vapor-phase material convection current of upwards flowing from more next reaction bed or stripping section by fractionating column. Carried out simultaneously the fractionation of catalytic reaction and product at this conversion zone vapour-liquid phase materials.
Fractionating column upper end will exceed the upper mounted plate certain altitude, forms a liquid layer at fixed head and makes uniformly inflow catalyst bed top of a part of liquid phase material, and the liquid phase material that all the other can not the inflow catalyst bed then overflows in the fractionating column.
Reaction raw materials can be entered in the tower by between the conversion zone bed, bottom the rectifying section or stripping section middle part according to reaction needed, react simultaneously at conversion zone and with fractionation reaction to be reached fully or till conversion ratio reaches requirement, reacted vapor phase product out returns cat head through condenser 14 condensation rear portions by cat head, and a part goes out device as product; Out a part is at the bottom of returning tower after reboiler 15 vaporization at the bottom of by tower for reacted liquid phase material, and a part goes out device as product.
Advantage of the present invention:
Simple in structure, loaded catalyst is large, loading and unloading easily, the vapour of reaction, liquid phase material can react effectively through conversion zone and the fractionation of product, reaction conversion ratio is high. Equipment of the present invention can be used for isobutene and the synthetic MTBE of methyl alcohol reaction, also can be used for MTBE and decomposes generation isobutene, C3～C
10Tertiary olefin and C1～C
4The reaction of alcohol generate relevant ethers, C3～C
10Hydrocarbon fraction is selected hydrogenation and removing diolefin and alkynes, tertiary olefin and water reaction to generate alcohols, alcohol and organic acid reaction and is generated ester class and other similar reactions.
Embodiment:
The catalytic distillation tower of the present invention that three fractionating columns are housed with the middle part is tested, the diameter 100mm of tower, the diameter 30mm of fractionating column.Upper rectifying section and bottom stripping section dress Φ 4 * 4mm stainless (steel) wire ring are filler, and Φ 4mm stainless steel ring filler also is housed in the fractionating column, are that catalyst is loaded between fractionating column with macropore sulfuric acid resin, with C
4Middle isobutene and methyl alcohol are that the synthetic MTBE (methyl tertiary butyl ether(MTBE)) of raw material reaction tests experimental condition and result of the test such as following table for example:
More than 4 groups of result of the test conversion ratios be more than 99%.
| Test | ?1????????2????????3????????4 |
| Isobutene content in the raw material, wt% alfin ratio mol/mol operating pressure MPa reflux ratio conversion zone temperature ℃ air speed h -1Isobutene conversion w% | 35.0?????36.0?????34.8?????34.8 1.2??????1.1??????1.15?????1.2 0.7??????0.7??????0.75?????0.75 1∶1?????1∶1?????1∶1?????1∶1 60～65???65～70???65～70???65～70 2.2??????2.3??????1.9??????1.85 99.0?????99.3?????99.5?????99.6 |
Claims (8)
1, a kind of shell and tube type catalytic distillation equipment is characterized in that conversion zone is made up of the fractionating column (7) of vertical arrangement and the catalyst between fractionating column.
2, catalysis-distillation equipment according to claim 1 is characterized in that having mouth on the fractionating column tube wall, tube wall outsourcing steel wire or pipe liner one deck net.
3, catalysis-distillation equipment according to claim 2 is characterized in that fractionating column can be circular, rectangle, and the tube wall opening can be the hole, strip ligulate opening.
4, according to claim 1,2,3 described catalysis-distillation equipments, it is characterized in that the fractionating column both ends open, in be filled with the fractionation filler.
5, catalysis-distillation equipment according to claim 1 is characterized in that fractionating column is fixed in the tower body by the fixed head at two ends, has perforate between the fractionating column of upper mounted plate.
6, according to claim 1,2,3 described catalysis-distillation equipments, the diameter that it is characterized in that circular fractionating column is 10～200mm, 30～80mm preferably, the width of rectangle fractionating column is 10～200mm, 30～80mm preferably, distance between the fractionating column is 5～100mm, is preferably 20～50mm.
7, catalysis-distillation equipment according to claim 1 is characterized in that the top in the tower body is rectifying section, and the bottom is a stripping section, and the middle part is a conversion zone.
8, catalysis-distillation equipment according to claim 1 is characterised in that conversion zone bed number is 1～10, is preferably 3～6.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN98110352A CN1074680C (en) | 1998-07-17 | 1998-07-17 | Shell and tube type catalytic distillation equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN98110352A CN1074680C (en) | 1998-07-17 | 1998-07-17 | Shell and tube type catalytic distillation equipment |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1242249A true CN1242249A (en) | 2000-01-26 |
| CN1074680C CN1074680C (en) | 2001-11-14 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN98110352A Expired - Fee Related CN1074680C (en) | 1998-07-17 | 1998-07-17 | Shell and tube type catalytic distillation equipment |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1074680C (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102701918A (en) * | 2012-06-11 | 2012-10-03 | 凯瑞化工股份有限公司 | Method for producing MTBE (Methyl Tert Butyl Ether) by taking gas phase isobutene as raw material |
| CN103480304A (en) * | 2013-09-06 | 2014-01-01 | 安徽淮化股份有限公司 | Nitric acid oxidation furnace with greenhouse gas emission reduction effect |
| CN104694150A (en) * | 2015-03-24 | 2015-06-10 | 天津大学 | Etherification, catalysis and rectification method and device for increasing gasoline octane number |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FI75741C (en) * | 1987-02-26 | 1988-08-08 | Santasalo Sohlberg Ab Oy | KOLONNKONSTRUKTION ELLER KOKUTRYMME I EN DESTILLATIONSANORDNING. |
| US5431890A (en) * | 1994-01-31 | 1995-07-11 | Chemical Research & Licensing Company | Catalytic distillation structure |
-
1998
- 1998-07-17 CN CN98110352A patent/CN1074680C/en not_active Expired - Fee Related
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102701918A (en) * | 2012-06-11 | 2012-10-03 | 凯瑞化工股份有限公司 | Method for producing MTBE (Methyl Tert Butyl Ether) by taking gas phase isobutene as raw material |
| CN103480304A (en) * | 2013-09-06 | 2014-01-01 | 安徽淮化股份有限公司 | Nitric acid oxidation furnace with greenhouse gas emission reduction effect |
| CN103480304B (en) * | 2013-09-06 | 2016-02-17 | 安徽淮化股份有限公司 | A kind of nitric acid oxidation furnace with reduction of greenhouse gas discharge effect |
| CN104694150A (en) * | 2015-03-24 | 2015-06-10 | 天津大学 | Etherification, catalysis and rectification method and device for increasing gasoline octane number |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1074680C (en) | 2001-11-14 |
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