CN1108844C - Fractionating reaction column plate type catalytic distillating equipment - Google Patents
Fractionating reaction column plate type catalytic distillating equipment Download PDFInfo
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- CN1108844C CN1108844C CN00110246A CN00110246A CN1108844C CN 1108844 C CN1108844 C CN 1108844C CN 00110246 A CN00110246 A CN 00110246A CN 00110246 A CN00110246 A CN 00110246A CN 1108844 C CN1108844 C CN 1108844C
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Abstract
The present invention discloses a fractionating reaction column plate type catalytic distilling device which is composed of a rectifying section at the upper part, a reaction section the middle part and a stripping section at the lower part. The present invention is characterized in that the reaction section is composed of one or a plurality of fractionating reaction column plates, and each fractionating reaction column plate is divided into two zones, namely a fractionating zone at the upper part and a reaction zone at the lower part; a conventional fractionating column plate is arranged between the second fractionating reaction column plates. Materials enters the reaction zones to generate reaction after being fractionated in the fractionating zones, the reaction materials is in direct contact with catalysts, and the reaction and the fractionation are alternatively carried out until the reaction is completely carried out so that the present invention has high reaction effect.
Description
Technical field:
The invention belongs to the catalysis-distillation equipment technical field, be specifically related to a kind of fractionating reaction column plate type catalytic distillating equipment.
Background technology:
Catalytic distillation technology is that grow up over nearly 20 years a kind of is combined in the novel petroleum chemical technology of carrying out in the equipment to reaction and fractional distillation process, because reaction and fractionation are combined in the equipment, so can react simultaneously and fractionation, in reaction, the product fractionation that generates is gone out, can promote the carrying out that reacts.Particularly for balanced reaction, in the time of owing to reaction product is separated, can be broken molecular balance, reaction is not subjected to the restriction of balance, thereby till can making reaction proceed to fully.
That catalytic distillation technology is begun to be widely used in petrochemical industry is american chemical reaction and the (CR﹠amp of chartered company; L company), the said firm is its process that is used for being generated by the isobutene of C 4 fraction and methyl alcohol reaction methyl tertiary butyl ether(MTBE) (MTBE), and 90 of the technology that isobutene conversion is separated by general reaction and fractionation carry out---95% brings up to more than 99.5%.CR﹠amp; The characteristics of L company catalytic distillation technology be catalyst packing in the tiny pocket made from the glass fiber strap, the glass fiber strap adds-and a layer wrinkle shape stainless steel cloth is rolled into the catalyst bag then, many this catalyst packings filled out on the gripper shoe of conversion zone in the middle part of the catalytic distillation tower.The free space that catalytic distillation tower middle part conversion zone vapor-phase material that upwards flows and the liquid material convection current that flows downward forms by wrinkle shape stainless steel cloth in the catalyst reaction section, reaction mass diffuses in the parcel and reacts, after the reaction again by diffusing out in the parcel, in the free space of catalyst bag, carry out fractionation, reaction and fractionation are carried out simultaneously, till reacting completely (US patent 4242530).The problem of this technology is not only must be catalyst packing in the glass wool cloth pouch, and to manually enter in the tower and load, also need manually enter taking-up one by one in the tower with the decaying catalyst of crossing, troublesome poeration, complex structure, and reaction mass need diffuse into could contact with catalyst in the catalyst pouch and react, and also need diffuse out the carrying out of influence reaction after the reaction.US patent 3434534 discloses a kind of catalytic distillation technology and catalyst is loaded in the downspout of board-like tower tray, and as an attached reactor, the catalyst loading amount is very little, and reaction is all low with fractionating efficiency, does not have industrial application value.US patent5348710 has introduced a kind of catalytic distillation technology, is characterized in the ventilative spacer member composition of conversion zone with inertia, every an interval loading catalyst, is empty vapour phase and liquid phase material convection channel between two catalyst.These catalyst elements are seated in the middle part conversion zone of catalytic distillation tower, from the vapour of upper rectifying section and bottom stripping section, liquid phase reacting material in convection current during by vapour phase and liquid channel, diffuse in the beds to contact and react with catalyst, reacted material enters vapour phase and liquid phase convection channel by diffusing out in the catalyst layer again, carries out fractionation therein.This technology reaction segment structure complexity, the manufacturing expense height also need manually enter in the tower and install, and also need manually enter taking-up in the tower behind the catalysqt deactivation.CN1048987A discloses a kind of catalytic distillation technology, be catalyst filling in many catalyst corbies, these corbies are installed on the distillation tower tray of catalytic distillation tower conversion zone, when flowing through plate, vapour phase and liquid phase material react simultaneously and fractionation, this structure also exists complex structure, and the manufacturing expense height manually enters loading and unloading catalyst corbie in the tower, reaction mass also will be through the problem of diffusion process, to reacting unfavorable.US patent 4847430 discloses a kind of catalytic distillation technology, be characterized in several bulk catalyst beds and the last distribution grid between two beds and following distribution grid of the middle part conversion zone of catalytic distillation tower, and in the middle of two distribution grids, be provided with two fractionating trays formations by overlapping placement.Catalyst is in bulk on the gripper shoe of beds, in the bed, is provided with vapor phase channel.Enter the beds top from the liquid phase material of the nethermost fractionating tray of catalytic distillation tower upper rectifying section and flow downward, pass beds, directly contact and react with catalyst.Reacted material is flowed out by the beds bottom, enter distribution grid, flow into two fractionating trays in centre below it by last distribution grid again, flow into distribution grid down then, come out to enter again next beds by following distribution grid, so hocket and react and fractionation, enter the fractionating tray at stripping section top after the nethermost catalyst bed reaction of process is complete.Reaction hockets with fractionation, reach requirement to conversion ratio till.This technology reaction mass can directly contact with catalyst, helps the carrying out that reacts.But complex structure will be established two distribution grids between per two beds, and two distillation trays can be full of beds for making reaction mass, also will establish fluid level controller on the beds, cause conversion zone height height, and investment is big.CN88109705.5 has also disclosed a kind of and US patent4847430 similar techniques improves to some extent in some aspects, but its operating principle is identical with US patent4847430.
Summary of the invention:
The purpose of this invention is to provide a kind of simple and reasonable for structure, cost is low, the fractionating reaction column plate type catalytic distillating equipment that distillation tray that reaction efficiency is high and reaction bed combine, solving the catalysis-distillation equipment complex structure that exists in the prior art, many deficiencies such as cost height, operation inconvenience, reaction efficiency are low.
The present invention adopts following technical scheme to realize: fractionating reaction column plate type catalytic distillating equipment is made up of upper rectifying section, middle part conversion zone and bottom stripping section.Be characterized in that the middle part conversion zone reacts column plates by one or several fractionation and forms.Each fractionation reaction column plate is divided into two zones: upward be fractionation zone, be reaction zone down.Fractionation zone is provided with conventional fraction elements.The reaction zone top is provided with the liquid phase material import, and the middle part is provided with conduit, and the bottom is the bulk catalyst bed.Upper rectifying section of this device and bottom stripping section are conventional fractionation structure.
The present invention is reasonable in design, and is simple in structure, and expenditure of construction is low, the height of conversion zone is low, catalyst filling rate (catalyst volume of conversion zone filling and the ratio of the cumulative volume of conversion zone) height, and reaction mass directly contacts the reaction efficiency height with the catalyst in beds in bulk.
Below in conjunction with accompanying drawing embodiments of the invention are described further.
Description of drawings:
Fig. 1 is the structural representation of embodiments of the invention one;
Fig. 2 is the A-A sectional view of Fig. 1;
Fig. 3 is the sectional view of the B-B of Fig. 1;
Fig. 4 is the structural representation of embodiments of the invention two;
Fig. 5 is A '-A ' sectional view of Fig. 4;
Fig. 6 is B '-B ' sectional view of Fig. 4.
The specific embodiment:
Catalytic distillation device of the present invention top is rectifying section 1, and the middle part is a conversion zone 2, and the bottom is a stripping section 3.Its rectifying section 1 and stripping section 3 are conventional fractionation structure.Conversion zone 2 is made of several fractionation reaction column plates 4.Each fractionation reaction column plate 4 is divided into two zones, promptly plays the fractionation zone 5 of fractionation and the reaction zone 6 of the effect of reacting.Fractionation zone 5 is provided with conventional fraction elements, as float valve, and bubble cap etc.Reaction zone 6 tops are liquid phase reacting material imports 7, and middle is the liquid phase reacting material of falling funnel-form conduit 8, and the bottom is the beds 9 that enlarges.Beds 9 tops are provided with catalyst loading port 12, and the bottom is provided with catalyst and unloads outlet 13, is used to load and unload catalyst.Establish catalyst gripper shoe 10 below the beds 9, its two side is a vapor phase channel 11.The liquid phase material import 7 at reaction zone top will be higher than fractionation reaction column plate 4, makes the liquid level of keeping certain height on the fractionation reaction column plate, to satisfy the requirement of fractionation.The liquid phase material import 7 at reaction zone top and the liquid phase material conduit 8 between the lower catalyst bed layer 9 also will have certain altitude, so that the supernatant layer of the liquid phase reacting material that beds is kept certain height above.The quantity of fractionation reaction column plate 4 and the catalyst amount in the beds 9 require to determine according to raw material composition and reaction conversion ratio in the conversion zone 2.Be provided with a conventional fractionating tray 15 between per two fractionation reaction column plate 4.
Several fractionation reaction column plates 4 of conversion zone 2 among Fig. 1 center symmetric arrangement successively in this device tower body.
Several fractionation reaction column plates 4 of conversion zone 2 among Fig. 4 interlaced arrangement successively in this device tower body.
The present invention is applicable to tertiary olefin and the synthetic ethers of alcohols reaction, and water and olefine reaction synthesize alcohols, and alcohols and organic acid reaction synthesizing ester, tertiary alcohols and ethers decompose other similar reactions such as producing high-purity alkene.Catalytic distillation device of the present invention top is rectifying section 1, and the middle part is a conversion zone 2, and the bottom is a stripping section 3.Reaction raw materials 14 enters on the fractionating tray 15 between two fractionation of conversion zone reaction column plate 4, liquid phase reacting material from rectifying section 1 a nethermost fractionating tray 16 enters on the fractionation zone 5 of fractionation reaction column plate 4, liquid phase material after this fractionation zone carries out fractionation enters the liquid phase reacting material import 7 of reaction zone 6, process intermediate conductor 8 flows downward and enters beds in bulk 9, contact with catalyst and to react, reacted reaction mass enters intermediate fractionation column plate 15 and further carries out fractionation from following fractionation reaction column plate vapor-phase material, and the product that reaction is generated is more complete with separating of unreacted reactant.Liquid phase material through this intermediate fractionation column plate 15 flows downward through downspout, enter next fractionation reaction column plate, further carry out fractionation and reagentia again, so repeatedly react fractionation and fractionation make enter the uppermost fractionating tray 17 of stripping section of conversion zone bottom after reacting completely after, each fractionating tray of stripping section that continues to flow through downwards conducts heat with vapor-phase material from the stripping section bottom, mass transport process, product is separated with all unreacted materials, heavy product is at last by coming out at the bottom of the tower, a part enters reboiler 18, upwards flow at the bottom of returning tower after the vaporization, enter conversion zone through stripping section, a part goes out device as product 19.The vapor-phase material that enters conversion zone through the vapor phase channel 11 of beds 9 both sides of conversion zone and the fractionating tray 15 between the fractionation reaction column plate 4 from conversion zone topmost the fractionation zone 5 of a fractionation reaction column plate 4 come out with from the backflow material convection current of cat head rectifying section 1 by catalytic distillation tower top, after advancing cooler 20 coolings, cat head enters return tank 21, a part is returned cat head as the backflow material, and a part goes out device as low boiling product 22.
Equipment of the present invention can be used for by C4-C8 tertiary olefin and the synthetic ethers of C1-C4 alcohol reaction, as reacting synthesize methyl tert-butyl ether (MTBE) by isobutene in catalysis C4 or the c4 cleavage cut and methyl alcohol, uncle's amylene in the catalysis C 5 fraction and methyl alcohol reaction synthesizing methyl tert-amyl ether (TAME), uncle's butylene in the light petrol, uncle's amylene, uncle be alkene and the synthetic ethers that mixes accordingly of methyl alcohol reaction, also can be used for decomposing the pure isobutene of generation, uncle's amylene by the tert-butyl alcohol, MTBE, TAMF, water and alkene or organic acid reaction generate alcohols and ester class, and other similar reactions.Be particularly suitable for being subjected to the chemical reaction of molecular balance restriction.Because the effect that its limit border ring is separated can be broken molecular balance, reaction is proceeded till reacting completely.See concrete application example:
Example 1: catalytic cracking C 4 fraction, isobutene content 16.5% and the synthetic MTBE of methyl alcohol reaction, alfin molecular proportion 1.05,65 ℃ of conversion zone mean temperatures.; Reflux ratio 1: 1, isobutene conversion 99.7%.
Example 2: catalytic cracking C5, uncle's amylene content 21% and the synthetic TAME of methyl alcohol reaction, alfin molecular proportion 1.1,67 ℃ of conversion zone mean temperatures, reflux ratio 1: 1, uncle's amylene conversion ratio 94.5%.
Example 3: by the uncle's amylene 10.9% in the catalytic cracking C5-C7 cut, uncle is alkene 9.8%, and uncle's heptene 6.6% mixes ethers accordingly, alfin molecular proportion 1.1,69 ℃ of conversion zone mean temperatures, reflux ratio 1: 1, tertiary olefin total conversion 67% with methyl alcohol reaction generation.
Claims (7)
1, a kind of fractionating reaction column plate type catalytic distillating equipment, by upper rectifying section (1), middle part conversion zone (2) is formed with bottom stripping section (3), it is characterized in that conversion zone (2) is made of one or several fractionation reaction column plates (4), each fractionation reaction column plate (4) is divided into two zones: upward be fractionation zone (5), be reaction zone (6) down; Reaction zone (6) top is provided with liquid phase material import (7), and the middle part is provided with conduit (8), and the bottom is bulk catalyst bed (9).
2, fractionating reaction column plate type catalytic distillating equipment according to claim 1 is characterized in that being provided with catalyst gripper shoe (10) below the beds (9), and its two side is vapor phase channel (11).
3, fractionating reaction column plate type catalytic distillating equipment according to claim 1 and 2 is characterized in that being provided with a conventional fractionating tray (15) between per two fractionation reaction column plates (4).
4, fractionating reaction column plate type catalytic distillating equipment according to claim 1 and 2 is characterized in that the liquid phase material import (7) at reaction zone (6) top will be higher than fractionation reaction column plate (4).
5, fractionating reaction column plate type catalytic distillating equipment according to claim 1 and 2 is characterized in that the liquid phase material import (7) at reaction zone (6) top and the liquid phase material conduit (8) between the lower catalyst bed layer (9) will have certain altitude.
6, fractionating reaction column plate type catalytic distillating equipment according to claim 1 and 2, several fractionation reaction column plates (4) that it is characterized in that conversion zone (2) center symmetric arrangement successively in this tower body.
7, fractionating reaction column plate type catalytic distillating equipment according to claim 1 and 2 is characterized in that several fractionation of conversion zone (2) reaction column plates (4) interlaced arrangement successively in this tower body.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN00110246A CN1108844C (en) | 2000-03-22 | 2000-03-22 | Fractionating reaction column plate type catalytic distillating equipment |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN00110246A CN1108844C (en) | 2000-03-22 | 2000-03-22 | Fractionating reaction column plate type catalytic distillating equipment |
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| Publication Number | Publication Date |
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| CN1281744A CN1281744A (en) | 2001-01-31 |
| CN1108844C true CN1108844C (en) | 2003-05-21 |
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| CN00110246A Expired - Fee Related CN1108844C (en) | 2000-03-22 | 2000-03-22 | Fractionating reaction column plate type catalytic distillating equipment |
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Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN101117614B (en) * | 2007-08-30 | 2010-12-08 | 宋永快 | Method for extracting fragrant liquor and essential oil from aromatic plants by dry-process |
| CN112316856B (en) * | 2020-09-01 | 2021-08-17 | 河北工业大学 | Equipment and method for producing ethylbenzene by catalytic reaction distillation with concentrated ethylene as raw material |
| CN114452901B (en) * | 2020-10-21 | 2023-03-07 | 中国石油化工股份有限公司 | Catalytic reaction unit and reactive distillation column |
| CN113019265B (en) * | 2021-03-16 | 2022-09-20 | 中国恩菲工程技术有限公司 | Reaction device and method for preparing final product by using same |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1042664A (en) * | 1988-11-24 | 1990-06-06 | 齐鲁石油化工公司研究院 | Catalytic distillation novel device and antigravity system |
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2000
- 2000-03-22 CN CN00110246A patent/CN1108844C/en not_active Expired - Fee Related
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1042664A (en) * | 1988-11-24 | 1990-06-06 | 齐鲁石油化工公司研究院 | Catalytic distillation novel device and antigravity system |
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| CN1281744A (en) | 2001-01-31 |
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