CN102188833B - Tower body of reaction distillation tower - Google Patents
Tower body of reaction distillation tower Download PDFInfo
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- CN102188833B CN102188833B CN2010101163455A CN201010116345A CN102188833B CN 102188833 B CN102188833 B CN 102188833B CN 2010101163455 A CN2010101163455 A CN 2010101163455A CN 201010116345 A CN201010116345 A CN 201010116345A CN 102188833 B CN102188833 B CN 102188833B
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Abstract
The invention relates to a tower body of a reaction distillation tower. The tower body mainly solves the problems that the conventional reaction distilling process is required to be realized by the reaction distillation tower and a product separation tower, the flow is complicated and energy consumption is high. The tower body of the reaction distillation tower comprises a raw material feeding hole, a feeding-side tower top feeding hole, a tower top discharge hole, a discharge-side tower top feeding hole, a discharge-side tower top discharge hole, a tower bottom feeding hole, a tower bottom discharge hole, a tower top separation plate, a reaction section, a discharge-side rectifying section and a common stripping section, wherein a rectifying section and/or a stripping section can be arranged on a feeding side; the separation plate in the tower body of the reaction distillation tower separates the tower into a feeding-side rectifying section, the reaction section, a feeding-side stripping section, the discharge-side rectifying section and the common stripping section; in a reaction distilling interval, the reaction section is positioned between the feeding-side rectifying section and the feeding-side stripping section, the feeding-side rectifying section is arranged above the reaction, and the feeding-side stripping section is arranged below the reaction section; an area between the bottom of the separation plate and the tower bottom feeding and discharge holes is the common stripping section; and in the area where the separation plate is located, the discharge-side rectifying section is arranged on the other side of the raw material feeding hole. By the technical scheme, the problems are better solved, and the tower body of the reaction distillation tower can be applied to reaction distilling industries.
Description
Technical field
The present invention relates to a kind of reactive distillation column tower body.
Background technology
Catalytic distillation technology is that reaction is carried out in same catalysis-distillation equipment with separation of products, when reaction is carried out, the separation of products generated is gone out, 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 generally forms by three sections: top is rectifying section (at the quality requirement to overhead product not high or can not establish rectifying section while not requiring), and middle part is catalyst reaction section, and bottom is stripping section.In catalytic distillation tower, the liquid phase material flowed downward must also be reacted and the product fractionation by the middle part catalyst reaction section therein with the mobile vapor-phase material that makes progress simultaneously in convection current.Chinese patent literature CN1380273A has introduced current methyl acetate catalysis rectification hydrolysis technique, and this technique mainly is comprised of catalytic rectifying tower, extractive distillation column, dealcoholize column, degreasing tower and azeotropy rectification column, and catalytic distillation is realized in different towers from product separation.At present common catalytic distillation technology flow chart is shown in Fig. 4, and according to the characteristics of reaction, the reaction distillation column overhead can the extraction light component, also can infinite reflux, there is the complicated and high problem of energy consumption of flow process.
Separate the tower development and come from the Petlyuk tower, the effect integrated by place a vertical next door generation pre-separation tower and king-tower at the king-tower interlude, in theory, be embedded in several separable five kinds of even more kinds of components in next door at a tower.For the thermal coupling distillation process, pre-separation tower and king-tower link together by gas-liquid flow, and centre is not provided with condenser and reboiler, at the bottom of tower top, tower and sideline product from the king-tower extraction, if there is no azeotropic mixture, side line also can obtain high purity product.With serial tower, compare, the thermal coupling tower is reduced investment not only, and efficiency is high, because separation component back-mixing in the minimizing of reboiler and condenser and distillation process disappears.CN1177513A has introduced a kind of destilling tower of the bulkhead type for the multicomponent mixture continuous rectification (separating tower), this destilling tower utilization distillation is separated into three kinds or multicomponent more by a mixture, and wherein at least one partition wall is detachably to be arranged in the bulkhead type destilling tower.
Therefore, separate tower technology and be applied in the reaction distillation process, can substitute reactive distillation column and the solvent recovery tower of traditional handicraft, there is flow process simply and the low characteristics of energy consumption.
Summary of the invention
Technical problem to be solved by this invention is to need reactive distillation column and product separation tower two towers to realize in current reaction distillation technique, there are flow process complexity and the high problem of energy consumption, a kind of new reactive distillation column tower body is provided, and the method has flow process simply and the low characteristics of energy consumption.
For solving the problems of the technologies described above, the technical solution used in the present invention is as follows, a kind of reactive distillation column tower body, comprise material inlet, feed side tower top charging aperture, the tower top discharging opening, extraction side tower top charging aperture, extraction side tower top charging aperture, charging aperture at the bottom of tower, discharging opening at the bottom of tower, the tower top demarcation strip, conversion zone, extraction side rectifying section, and public stripping section, wherein feed side can arrange rectifying section and/or stripping section, in the reactive distillation column tower body, demarcation strip is separated into the feed side rectifying section by tower, conversion zone, the feed side stripping section, extraction side rectifying section, and public stripping section, in the reaction distillation interval, conversion zone is between feed side rectifying section and feed side stripping section, and the conversion zone top is the feed side rectifying section, and the conversion zone below is the feed side stripping section, at the bottom of demarcation strip bottom and tower between feed inlet and outlet zone be public stripping section, demarcation strip region material inlet opposite side is extraction side rectifying section.
In technique scheme, material inlet is at least one; Material inlet is positioned at the reaction distillation interval, and demarcation strip is until separate column overhead; When reactive distillation column is applied to methyl acetate hydrolysis, it is 10～80 that conversion zone is equivalent to number of theoretical plate, and extraction side theoretical number of plates of rectifying section is 10～80, and public stripping section number of theoretical plate is 10～50, and the control temperature of extraction side tower top is 64.3～64.7 ℃.
In some reaction distillation process, reactant and product can form three strands of cuts according to boiling point difference, and reactive distillation column can only be cut to two strands of cuts, expect three strands of cuts, must introduce the product separation tower.And, in some system, reactive distillation column is a realization response function in essence, the tower top infinite reflux, reactant and product separation are realized in the product separation tower, so traditional handicraft is necessary for the combined process flow of reactive distillation column and product separation tower.In the present invention, reactive distillation column can complete separately reaction distillation and product separation process, realizes the effect of two tower unifications, with traditional handicraft, compares, and flow process is simple, i.e. reactive distillation column alternative reaction destilling tower and product separation tower.Use the present invention in the situation that water and methyl acetate mol ratio 3.0, reaction temperature are that the operating conditions such as 50～60 ℃, number of theoretical plate 58 are identical, total energy consumption saving 13.7%, obtained technique effect preferably.
The accompanying drawing explanation
Fig. 1 is the reactive distillation column schematic diagram.
Fig. 2 is the A-A view in Fig. 1.
Fig. 3 is the B-B view in Fig. 1.
Fig. 4 is that classical inverse is answered the distil process flow chart.
In Fig. 1,2 and 3,1 is reactive distillation column, and 2 is material inlet, 3 feed side tower top discharging openings, 4 is feed side tower top charging aperture, 5 is discharging opening at the bottom of extraction side tower, 6 is charging aperture at the bottom of extraction side tower, and 7 is discharging opening at the bottom of tower, and 8 is charging aperture at the bottom of tower, 9 is the feed side rectifying section, 10 is conversion zone, and 11 is the feed side stripping section, and 12 is public stripping section, 13 is extraction side rectifying section, and 14 is demarcation strip.
In Fig. 4,1 is reactive distillation column, and 2 is the product separation tower, and 3 and 4 is reactant feed, and 5 is light component, and 6 is the mixture cut, and 7 is midbarrel, and 8 is heavy distillat.
As shown in Figure 4,3 and 4 reaction raw materials enter the reaction distillation charging aperture from the charging aperture of reactive distillation column, in the conversion zone reaction, separated, overhead condenser connects the tower top feed inlet and outlet, after the tower top outlet steam-condensation, carry out infinite reflux, perhaps first sends into the tower top import, and the second portion extraction is as light component 5, and at the bottom of tower, mixed fraction 6 enters the product separation tower, overhead extraction midbarrel 7, obtain heavy distillat 8 at the bottom of tower.
Below by specific embodiment, the present invention is further illustrated, and still, scope of the present invention has more than and is limited to the scope that embodiment covers.
The specific embodiment
[embodiment 1]
Press reactive distillation column shown in Fig. 1, public stripping section number of theoretical plate is 15, it is 18 that the conversion zone separative efficiency is equivalent to number of theoretical plate, the feed side theoretical number of plates of rectifying section is 5, feed side stripping section number of theoretical plate is 10, extraction side theoretical number of plates of rectifying section is 25, catalyst is sulfonate sodium type ion exchange resin, water enters with 2.32 gram/minute flows the 1st theoretical plate separating the tower conversion zone and (counts from top to bottom, as follows), methyl acetate enters from separating tower conversion zone bottom with 3.00 gram/minute flows, controlling separation tower extraction side tower top temperature is 64.5 ℃, extraction side overhead extraction amount is 1.30 gram/minute, after stable operation, acquired results is that extraction side tower top methanol content is 99.97 % by weight, at the bottom of tower, acetic acid content is 60.45 % by weight, feed side overhead condenser energy consumption-1.17 kilojoule/hour, extraction side overhead condenser energy consumption-0.46 kilojoule/hour, the tower bottom reboiler energy consumption be 2.34 kilojoules/hour, total energy consumption descends 13.7%.
[embodiment 2]
Press reactive distillation column shown in Fig. 1, public stripping section number of theoretical plate is 30, it is 25 that the conversion zone separative efficiency is equivalent to number of theoretical plate, the feed side theoretical number of plates of rectifying section is 15, feed side stripping section number of theoretical plate is 20, extraction side theoretical number of plates of rectifying section is 30, catalyst is sulfonate sodium type ion exchange resin, water enters with 2.32 gram/minute flows the 1st theoretical plate separating the tower conversion zone and (counts from top to bottom, as follows), methyl acetate enters from separating tower conversion zone bottom with 3.00 gram/minute flows, controlling separation tower extraction side tower top temperature is 64.5 ℃, the overhead extraction amount is 1.30 gram/minute, after stable operation, acquired results is that extraction side tower top methanol content is 99.92 % by weight, at the bottom of tower, acetic acid content is 60.41 % by weight, feed side overhead condenser energy consumption-1.13 kilojoule/hour, extraction side overhead condenser energy consumption-0.46 kilojoule/hour, the tower bottom reboiler energy consumption be 2.30 kilojoules/hour.
[embodiment 3]
Press reactive distillation column shown in Fig. 1, public stripping section number of theoretical plate is 10, it is 10 that the conversion zone separative efficiency is equivalent to number of theoretical plate, extraction side theoretical number of plates of rectifying section is 10, catalyst is sulfonate sodium type ion exchange resin, water enters with 2.32 gram/minute flows the 1st theoretical plate separating the tower conversion zone and (counts from top to bottom, as follows), methyl acetate enters from separating tower conversion zone bottom with 3.00 gram/minute flows, controlling separation tower extraction side tower top temperature is 64.5 ℃, the overhead extraction amount is 1.30 gram/minute, after stable operation, acquired results is that extraction side tower top methanol content is 99.92 % by weight, at the bottom of tower, acetic acid content is 60.41 % by weight, feed side overhead condenser energy consumption-1.26 kilojoule/hour, extraction side overhead condenser energy consumption-0.49 kilojoule/hour, the tower bottom reboiler energy consumption be 2.52 kilojoules/hour.
[comparative example 1]
Press technological process shown in Fig. 4, the reactive distillation column number of theoretical plate be the conversion zone separative efficiency to be equivalent to number of theoretical plate be 18, the stripping section number of theoretical plate is 15, product separation tower theoretical number of plates of rectifying section is 15, the stripping section number of theoretical plate is 15.The 1st theoretical plate that water enters the reactive distillation column conversion zone with 2.32 gram/minute flows (counted from top to bottom, as follows), methyl acetate enters from reactive distillation column conversion zone bottom with 3.00 gram/minute flows, the tower top infinite reflux, full extraction at the bottom of tower, at the bottom of tower, Produced Liquid enters product separation tower middle part, controlling product separation column overhead temperature is 64.5 ℃, the overhead extraction amount is 1.30 gram/minute, after stable operation, acquired results is that extraction side tower top methanol content is 99.98 % by weight, at the bottom of tower, acetic acid content is 60.47 % by weight, reactive distillation column overhead condenser energy consumption-1.34 kilojoule/hour, tower bottom reboiler energy consumption 1.89 kilojoules/hour, product separation column overhead condenser energy consumption-0.55 kilojoule/hour, tower bottom reboiler energy consumption 0.82 kilojoule/hour.
Claims (1)
1. a reactive distillation column tower body, comprise material inlet, feed side tower top charging aperture, the tower top discharging opening, extraction side tower top charging aperture, extraction side tower top charging aperture, charging aperture at the bottom of tower, discharging opening at the bottom of tower, tower top demarcation strip, conversion zone, extraction side rectifying section, and public stripping section, wherein feed side arranges rectifying section and/or stripping section, and in the reactive distillation column tower body, demarcation strip is separated into feed side rectifying section, conversion zone by tower, the feed side stripping section, extraction side rectifying section, and public stripping section; In the reaction distillation interval, conversion zone is between feed side rectifying section and feed side stripping section, and the conversion zone top is the feed side rectifying section, and the conversion zone below is the feed side stripping section; At the bottom of demarcation strip bottom and tower between feed inlet and outlet zone be public stripping section, demarcation strip region material inlet opposite side is extraction side rectifying section;
Described reactive distillation column tower body is for the ethyl acetate hydrolysis, the public stripping section number of theoretical plate of described reactive distillation column is 30, it is 25 that the conversion zone separative efficiency is equivalent to number of theoretical plate, the feed side theoretical number of plates of rectifying section is 15, feed side stripping section number of theoretical plate is 20, extraction side theoretical number of plates of rectifying section is 30, catalyst is sulfonate sodium type ion exchange resin, water enters and separates tower conversion zone the 1st theoretical plate of number from top to bottom with 2.32 gram/minute flow, methyl acetate enters from separating tower conversion zone bottom with 3.00 gram/minute flows, controlling separation tower extraction side tower top temperature is 64.5 ℃, the overhead extraction amount is 1.30 gram/minute, after stable operation, acquired results is that extraction side tower top methanol content is 99.92 % by weight, at the bottom of tower, acetic acid content is 60.41 % by weight, feed side overhead condenser energy consumption-1.13 kilojoule/hour, extraction side overhead condenser energy consumption-0.46 kilojoule/hour, the tower bottom reboiler energy consumption be 2.30 kilojoules/hour.
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| CN2010101163455A CN102188833B (en) | 2010-03-03 | 2010-03-03 | Tower body of reaction distillation tower |
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| CN102188833B true CN102188833B (en) | 2013-12-04 |
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Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1177513A (en) * | 1996-04-30 | 1998-04-01 | 巴斯福股份公司 | Separated-wall type distillation tower for continuous distillation of multi-component mixture |
| CN101244982A (en) * | 2008-01-31 | 2008-08-20 | 中国石油大学(华东) | Hydrolyzation separation apparatus for methyl acetate and technique |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| TW200738602A (en) * | 2006-02-01 | 2007-10-16 | Asahi Kasei Chemicals Corp | Industrial process for producing high-purity diol |
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Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1177513A (en) * | 1996-04-30 | 1998-04-01 | 巴斯福股份公司 | Separated-wall type distillation tower for continuous distillation of multi-component mixture |
| CN101244982A (en) * | 2008-01-31 | 2008-08-20 | 中国石油大学(华东) | Hydrolyzation separation apparatus for methyl acetate and technique |
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| CN102188833A (en) | 2011-09-21 |
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