CN106699566A - Method for coproducing ethyl acetate and n-butyl acetate by reactive distillation dividing wall column - Google Patents
Method for coproducing ethyl acetate and n-butyl acetate by reactive distillation dividing wall column Download PDFInfo
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- CN106699566A CN106699566A CN201710030652.3A CN201710030652A CN106699566A CN 106699566 A CN106699566 A CN 106699566A CN 201710030652 A CN201710030652 A CN 201710030652A CN 106699566 A CN106699566 A CN 106699566A
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- C07C67/00—Preparation of carboxylic acid esters
- C07C67/08—Preparation of carboxylic acid esters by reacting carboxylic acids or symmetrical anhydrides with the hydroxy or O-metal group of organic compounds
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- C07C67/52—Separation; Purification; Stabilisation; Use of additives by change in the physical state, e.g. crystallisation
- C07C67/54—Separation; Purification; Stabilisation; Use of additives by change in the physical state, e.g. crystallisation by distillation
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Abstract
The invention relates to a method for coproducing ethyl acetate and n-butyl acetate by a reactive distillation dividing wall column. The method adopts a reactive distillation dividing wall column, the raw material ethanol is fed from the bottom of the reaction section, and the raw materials n-butanol and acetic acid are fed from the middle part of the reaction section; and the two reactions are arranged in one reaction region, so the n-butyl acetate can be used as an azeotrope former for producing water in the ethyl acetate preparation process when being used for preparing ethyl acetate-n-butyl acetate, thereby reducing the reflux quantity of the column top ethyl acetate, enhancing the reaction conversion rate, lowering the contents of ethanol and water in the column top ester phase, and lowering the energy consumption in the production process. The method can reduce the amounts of the condensers and reboilers and enhance the thermodynamic efficiency, thereby lowering the energy consumption of distillation, implementing deep energy conservation and bringing in favorable economic benefits.
Description
Technical field
The present invention relates to a kind of utilization reactive distillation next door tower coproduction ethyl acetate and the technique of n-butyl acetate, specifically
With ethanol, n-butanol and acetic acid as raw material, realize preparing and clear separating ethyl acetate and the positive fourth of acetic acid in single rectifying column
The technique of ester.
Background technology
In the production process of the industries such as oil, chemical industry, energy consumption of rectification accounts for 40% or so of whole process energy consumption, therefore
Realizing the energy-saving and emission-reduction of distillation process has important social effect.Reactive distillation next door tower is a kind of by reactive distillation and next door
Tower-coupled Novel hot coupled, has broken reaction balance and the limitation that balances each other, and reduces the back-mixing degree of intermediate species, can show
Writing reduces separating energy consumption.Ethyl acetate and n-butyl acetate are all important organic solvents in Chemical Manufacture, are widely used in oil
The industries such as paint, spices and weaving.Traditional reactive distillation esterification process production ethyl acetate, the method are commonly used in current domestic industry
On the one hand substantial amounts of ester is needed to take in tower the water of generation out of in overhead reflux, the thick ester reclaimed water of another aspect tower top and ethanol contain
Amount is higher, makes the vapour-liquid load that subsequent separation process needs are higher, so energy consumption is higher.The production of n-butyl acetate simultaneously needs
By aqueous-phase reflux to take the n-butyl acetate of generation out of, therefore energy consumption is also higher.
Miguel A.Santaella et al. propose that reactive distillation next door tower prepares ethyl acetate in the literature, in prefractionation
Duan Fasheng esterifications, public rectifying section tower top distillates thick ethyl acetate, main column section tower reactor extracted waste water.But process program master
Lean on tower top ester mutually to flow back and take the water of reaction generation out of, reflux ratio is larger, therefore tower reactor energy consumption is also corresponding higher.Zhang Bingjian et al.
Ethyl acetate is prepared using reactive distillation, addition n-butyl acetate is that entrainer goes out the water for reacting generation from side line Bian, one
Determine to reduce tower top ester phase capacity of returns and tower reactor energy consumption in degree, but due to the back-mixing problem of intermediate species, so its thermodynamics
It is less efficient.Tian Hui et al. proposition ethyl acetate and n-butyl acetate technique, two reactive distillation columns of technique needs (including two
Platform condenser, two reboilers), preparative separation ethyl acetate and n-butyl acetate respectively have that cost of equipment is high, flow is complicated
The problems such as.
In sum, ethyl acetate and n-butyl acetate production technology have that flow is complicated, thermodynamic efficiency is low, high energy consumption
The problems such as, therefore it is particularly important to find the process program that a kind of flow is simple, thermodynamic efficiency is high, energy consumption is low.
The content of the invention
The invention provides a kind of reactive distillation next door tower coproduction ethyl acetate and the technique of n-butyl acetate, it is therefore an objective to solve
The problems such as certainly traditional reactive distillation production ethyl acetate, n-butyl acetate separation process complexity, high energy consumption, investment high.The technique
Two reactions are placed on same conversion zone, while ethyl acetate acetic acid N-butyl is prepared, n-butyl acetate can also fill
The entrainer of water is produced when ethyl acetate is prepared, so as to reduce the capacity of returns of tower top ethyl acetate, reaction conversion ratio, drop is improved
The content of second alcohol and water in low tower top ester phase, reduces the energy consumption of production process.Another aspect present invention process may be implemented in single
Rectifying column in prepare and clear separating ethyl acetate and n-butyl acetate, can not only reduce condenser and reboiler consumption, and
And its thermodynamic efficiency can be lifted, and energy consumption of rectification is further reduced, depth energy-conservation is realized, bring good economic benefit.
The technical scheme is that：
A kind of method of reactive distillation next door tower coproduction ethyl acetate and n-butyl acetate, comprises the following steps：
In described reactive distillation next door tower, dividing plate is located on the central axis in tower, and prefractionation section is located at dividing plate left side,
Public rectifying section is located at dividing plate top；Main column section is located at dividing plate right side, and public stripping section is located at the lower partition；Material is in prefractionation
Section middle part feeds and reacts, and is considered as conversion zone；Storng-acid cation exchange resin Amberlyst15 is housed in conversion zone,
Loadings are 0.6~1kg/L fillers；
Described reactive distillation next door tower is atmospheric operation；Bottom temperature is 114~117 DEG C；
(1) from the bottom feed of conversion zone, raw material n-butanol and acetic acid feed feed ethanol from the middle part of conversion zone；Second
There is esterification in alcohol, n-butanol and acetic acid, ethyl acetate and n-butyl acetate are generated respectively, then A, B component in conversion zone
Public rectifying section is upwardly into, B, component C are downwardly into public stripping section；
Wherein, component A is ethyl acetate, the ternary azeotrope of second alcohol and water；B component is the binary of n-butyl acetate and water
Azeotropic mixture；Component C is the mixture of acetic acid and water, and wherein acetic acid concentration is more than 95%wt；
(2) A, B component described in sequentially pass through public rectifying section and the top of main column section is realized separating；Component A enters tower
Push up condensed device and be condensed into liquid phase, enter back into the first phase-splitter split-phase, the upper strata of the first phase-splitter is that ethyl acetate content is 93
The ester phase of~95%wt, lower floor is the water phase that water content is 90~92%wt；Ester mutually part extraction a, part is back in tower
Public rectifying section, ester phase reflux ratio is 2.5-4；Water mutually part extraction a, part is back to public rectifying section in tower, and water phase is returned
Stream ratio is 0.4-0.65；And B component enters the top half of main column section；
(3) B, component C described in sequentially pass through public stripping section and the bottom of main column section is realized separating；Wherein component C is entered
Enter the bottom of public stripping section, from tower reactor extraction；And remaining B component is then into the latter half of main column section, and from king-tower
The B component of part is converged in the middle part of main column section together in section, then sideline product extraction, and sideline product is cold through side line condenser
After solidifying, the second phase-splitter split-phase is entered back into, the upper strata in the second phase-splitter is the ester that n-butyl acetate content is 89~92%wt
Phase, lower floor is the water phase that water content is 90~92%wt；
Three kinds of feedstock temperature are 40-50 DEG C；The mole of feed ratio of ethanol and n-butanol is 3-4:1；Acetic acid with
The mole of feed ratio of ethanol is 1.2-2：1；The concentration of feed ethanol is 95%wt；Raw material butanol concentration is 100%wt；Raw material
The concentration of acetic acid is 80%-100%wt；
The number of theoretical plate of described prefractionation section is 20-40；The number of theoretical plate of public rectifying section is 5-15；The reason of main column section
It is 20-40 by plate number；The number of theoretical plate of public stripping section is 5-15；Conversion zone is on prefractionation section 10-30 block theoretical plates；
The feed entrance point of described feed ethanol is 10~20 blocks of column plates of prefractionation section；Described raw material n-butanol and second
The feed entrance point of acid is 15~30 blocks of column plates of prefractionation section；Managed for the 10-25 blocks of main column section the extraction position of sideline product
By plate；
Both sides of the decline liquid phase of public rectifying section at the top of dividing plate proportionally 0.48-2.3：1 is allocated, and enters respectively
Enter prefractionation section and main column section；
Both sides proportionally 0.48-2.3 of the rising vapour phase of public stripping section in dividing plate bottom：1 is allocated, and enters respectively
Enter prefractionation section and main column section；
Described reactive distillation next door tower is preferably packed tower.
Compared with prior art, the beneficial effects of the invention are as follows：
The present invention utilize reactive distillation next door tower coproduction ethyl acetate and n-butyl acetate, carry out reactive distillation next door tower and
The process intensification of joint production process, may be implemented in and prepared in single rectifying tower and clear separating ethyl acetate and n-butyl acetate.
The present invention can adjust reactant ethanol and positive fourth according to market for the demand of ethyl acetate and n-butyl acetate
The ratio of alcohol, so as to obtain the ethyl acetate and n-butyl acetate product of the amount of according with the demands of the market.
The present invention can be according to the purity of acetic acid raw material, sweetly disposition tower reactor logistics, when acetic acid raw material concentration is 80-90%wt
When, present invention process can realize the refined of acetic acid by public stripping section while coproduction ethyl acetate and n-butyl acetate,
Can be in tower reactor acetic acid product of the extraction concentration more than 95%wt；When acetic acid raw material concentration is 90-100%wt, tower reactor logistics is not
Extraction, but acetic acid feed mouthful is returned it into by pump and is circulated utilization.
This process program change reactant ethanol and n-butanol charge proportion, reactant acetic acid concentration etc. under the conditions of, with
Traditional reactive distillation process project plan comparison is capable of achieving to save energy consumption 30% or so.
Brief description of the drawings
Fig. 1 is the schematic flow sheet of reactive distillation next door tower coproduction ethyl acetate acetic acid dinbutyl phthalate technology
Specific embodiment
The present invention is further described with reference to embodiment and accompanying drawing.
For the present invention is better described, technical scheme is readily appreciated, it is of the invention typical but non-limiting
Embodiment is as follows：
The method of reactive distillation next door tower coproduction ethyl acetate of the present invention and n-butyl acetate, as shown in figure 1, every
Plate is located on the central axis in tower, and prefractionation section I is located at dividing plate left side, and number of theoretical plate is 30；Public rectifying section II be located at every
Plate top, number of theoretical plate is 10；Main column section III is located at dividing plate right side, and number of theoretical plate is 30；Public stripping section IV is located under dividing plate
Portion, number of theoretical plate is 10；Conversion zone V prefractionation section I 10-20 block theoretical plates on, equipped with strongly acidic cation exchange tree
Fat Amberlyst15, wherein filling 0.8kg catalyst in every liter of filler.
Reactive distillation next door tower is packed tower, and filler is the Dixon ring of 3*3.Operating pressure is 101.325kPa.Feed ethanol
From the 20th block of plate charging of prefractionation section I, raw material n-butanol and acetic acid feed from the 15th block of plate of prefractionation section I；Ethanol, positive fourth
There is esterification in alcohol, ethyl acetate and n-butyl acetate are generated respectively with acetic acid in conversion zone V, wherein, ethyl acetate, second
The ternary azeotrope of alcohol and water is component A, and the binary azeotrope of n-butyl acetate and water is the mixture of B component, acetic acid and water
It is component C, wherein acetic acid concentration is more than 95%wt.
The specific separating step of product is as follows after reaction：
A, B component are realized clearly separating with B, component C in prefractionation section I, i.e., A, B enter public rectifying section II, and B, C enter
Enter public stripping section IV.
A, B component realize clear separation on the top of public rectifying section II and main column section III.Wherein component A is cold into tower top
Condenser C-101 (condenser temperature is 35 DEG C) is condensed into liquid phase, and phase-splitter D-101 is entered back into afterwards carries out split-phase, and upper strata is ester
Phase (ethyl acetate content is about 94%wt), lower floor is water phase (water content is about 91%wt).Ester mutually part extraction, a part
It is back in tower；It is acetic acid content (acetic acid content is less than 0.03%wt) in control tower top and sideline product, need to be by aqueous portion
Backflow.And remaining B component enters the top half of main column section III.
B, component C realize clear separation in the bottom of public stripping section IV and main column section III.Wherein component C is from public stripping
The bottom extraction (acetic acid content is more than 95%wt) of section IV, and remaining B component is then into the latter half of main column section III and master
The B component of part is together as sideline product extraction in tower section III (n-butyl acetate content is about 78%wt).Sideline product B groups
After lease making condenser C-102 (condenser temperature is 35 DEG C) condensation, phase-splitter D-102 split-phases are entered back into, upper strata is the positive fourth of acetic acid
Ester crude product (n-butyl acetate content is about 90%wt), lower floor is water phase (water content is about 90%wt).
Feedstock temperature is between 40-50 DEG C；The mole of feed ratio of ethanol and n-butanol is 3-4:1；Acetic acid and second
The raw materials components mole ratio example of alcohol is 1.2-2：1；The concentration of feed ethanol is 95%wt；Raw material butanol concentration is 100%wt；Raw material second
The concentration of acid is 80%-100%wt.
Pre- point in dividing plate both sides of the rising vapour phase proportional assignment of the decline liquid phase of public rectifying section and public stripping section
Evaporate in section and main column section, carry out reverse contact and realize mass transfer separation process.Wherein by controlling swinging funnel two at the top of dividing plate
The duration of oscillation of side controls liquid phase distribution ratio for 0.3-0.7, and wherein liquid phase distribution ratio is the liquid phase flow into prefractionation section
With the ratio of total liquid phase flow；Vapour phase distribution ratio is controlled by balancing the pressure drop of dividing plate both sides for 0.3-0.7, wherein vapour phase distribution
Than for into the ratio of vapour phase flow and total vapour phase flow of prefractionation section.
Ester phase reflux ratio is 2.5-4；Wherein ester phase reflux ratio is the ratio of tower top ester phase produced quantity and capacity of returns.
Aqueous-phase reflux ratio is 0.4-0.65；Wherein aqueous-phase reflux ratio is overhead water phase produced quantity and water phase total flow
Ratio.
Acetic acid raw material concentration depends on factory's actual production situation, when acetic acid raw material concentration is 80%-90%wt, makes anti-
Answer thing acetic acid with respect to ethanol and butanol excess 20%-100%, do not participate in the acetic acid of reaction through prefractionation section I and public stripping section
IV refine, acetic acid product of the concentration more than 95%wt is directly produced in tower reactor, that is, realize the refined concentrate of raw acetic acid.Work as second
When acid starting material concentration is 90%-100%wt, then make reactant ethanol excessive with respect to acetic acid 3%, through prefractionation section I and public carry
The separation of section IV is evaporated, tower reactor is acetic acid stream of the concentration more than 95%wt, and the logistics is not produced but returns it into second by pump
Sour feed cycle is used.
Case study on implementation 1
Reactive distillation next door tower is packed tower, and tower diameter is 0.43m, and dividing plate is located on the central axis in tower, prefractionation section I
Number of theoretical plate be 30, number of theoretical plate that the number of theoretical plate of public rectifying section II is 10, main column section III be 30, public stripping section IV
Number of theoretical plate be 10, conversion zone V prefractionation section I 10-20 block theoretical plates.The operating pressure of reactive distillation next door tower
It is 101.325kPa, bottom temperature is 115 DEG C.Feed ethanol is from the 20th block of plate charging of prefractionation section I, raw material n-butanol and second
From the 15th block of plate charging of prefractionation section I, side take-off position is the 15th piece of theoretical plate of main column section for acid.Feeding temperature is in 40-
Between 50 DEG C.The concentration of acetic acid raw material is 100%wt, and feed rate is 5kmol/h.Ethanol raw material concentration is 95%wt, charging
Flow is 4kmol/h；N-butanol material concentration is 100%wt, and feed rate is 1kmol/h.Liquid phase distribution ratio is 0.6；Vapour phase
Distribution ratio is 0.5；Tower top ester phase reflux ratio is 3；Overhead water mutually flows back ratio for 0.45.Ethyl acetate in tower top ester phase product
Mass concentration is 93.8%；The mass concentration of overhead water phase reclaimed water is 91.4%；The matter of n-butyl acetate in side line ester phase product
Amount concentration is 90.2%；The mass concentration of side line water phase reclaimed water is 90.7%.Tower reactor energy consumption is 280kw, is reacted compared to tradition
Rectifying column prepares ethyl acetate technique and saves tower reactor energy consumption 34%.
Case study on implementation 2
Reactive distillation next door tower is packed tower, and tower diameter is 0.43m, and dividing plate is located on the central axis in tower, prefractionation section I
Number of theoretical plate be 30, number of theoretical plate that the number of theoretical plate of public rectifying section II is 10, main column section III be 30, public stripping section IV
Number of theoretical plate be 10, conversion zone V prefractionation section I 10-20 block theoretical plates.The operating pressure of reactive distillation next door tower
It is 101.325kPa, bottom temperature is 117 DEG C.Feed ethanol is from the 20th block of plate charging of prefractionation section I, raw material n-butanol and second
From the 15th block of plate charging of prefractionation section I, side take-off position is the 15th piece of theoretical plate of main column section for acid.Feeding temperature is in 40-
Between 50 DEG C；The concentration of acetic acid raw material is 85%wt, and feed rate is 8kmol/h.Ethanol raw material concentration is 95%wt, enters stream
It is 4kmol/h to measure；N-butanol material concentration is 100%wt, and feed rate is 1kmol/h.Liquid phase distribution ratio is 0.63；Vapour phase point
Match is 0.5；Tower top ester phase reflux ratio is 2.8；Overhead water mutually flows back ratio for 0.42.Ethyl acetate in tower top ester phase product
Mass concentration is 93.1%；The mass concentration of overhead water phase reclaimed water is 90.8%；The matter of n-butyl acetate in side line ester phase product
Amount concentration is 89.9%；The mass concentration of side line water phase reclaimed water is 90.1%.Tower reactor energy consumption is 302kw, is reacted compared to tradition
Rectifying column prepares ethyl acetate technique and saves tower reactor energy consumption 29%.
Case study on implementation 3
Reactive distillation next door tower is packed tower, and tower diameter is 0.38m, and dividing plate is located on the central axis in tower, prefractionation section I
Number of theoretical plate be 30, number of theoretical plate that the number of theoretical plate of public rectifying section II is 10, main column section III be 30, public stripping section IV
Number of theoretical plate be 10, conversion zone V prefractionation section I 10-20 block theoretical plates.The operating pressure of reactive distillation next door tower
It is 101.325kPa, bottom temperature is 117 DEG C.Feed ethanol is from the 20th block of plate charging of prefractionation section I, raw material n-butanol and second
From the 15th block of plate charging of prefractionation section I, side take-off position is the 15th piece of theoretical plate of main column section for acid.Feeding temperature is in 40-
Between 50 DEG C；The concentration of acetic acid raw material is 85%wt, and feed rate is 6kmol/h.Ethanol raw material concentration is 95%wt, enters stream
It is 3kmol/h to measure；N-butanol material concentration is 100%wt, and feed rate is 1kmol/h.Liquid phase distribution ratio is 0.66；Vapour phase point
Match is 0.5；Tower top ester phase reflux ratio is 3.1；Overhead water mutually flows back ratio for 0.51.N-butyl acetate in tower top ester phase product
Mass concentration be 93.9%；The mass concentration of overhead water phase reclaimed water is 91.7%；The matter of ethyl acetate in side line ester phase product
Amount concentration is 91.3%；The mass concentration of side line water phase reclaimed water is 91.6%.Tower reactor energy consumption is 264kw, is reacted compared to tradition
Rectifying column prepares ethyl acetate technique and saves tower reactor energy consumption 37.8%.
The present invention does not address part and is applied to prior art.
Claims (6)
1. a kind of method of reactive distillation next door tower coproduction ethyl acetate and n-butyl acetate, it is characterized by the method include it is following
Step：
In described reactive distillation next door tower, dividing plate is located on the central axis in tower, and prefractionation section is located at dividing plate left side, public
Rectifying section is located at dividing plate top, and main column section is located at dividing plate right side, and public stripping section is located at the lower partition；Material is in prefractionation section
Portion feeds and reacts, and is considered as conversion zone；Storng-acid cation exchange resin Amberlyst15, filling are housed in conversion zone
It is 0.6 ~ 1kg/L fillers to measure；
Described reactive distillation next door tower is atmospheric operation；Bottom temperature is 114 ~ 117 DEG C；
（1）From the bottom feed of conversion zone, raw material n-butanol and acetic acid feed feed ethanol from the middle part of conversion zone；Ethanol, just
There is esterification in butanol, ethyl acetate and n-butyl acetate are generated respectively with acetic acid in conversion zone, and then A, B component are to enterprising
Enter public rectifying section, B, component C are downwardly into public stripping section；
Wherein, component A is ethyl acetate, the ternary azeotrope of second alcohol and water；B component is the binary azeotropic of n-butyl acetate and water
Thing；Component C is the mixture of acetic acid and water, and wherein acetic acid concentration is more than 95%wt；
（2）Described A, B component sequentially pass through public rectifying section and the top of main column section is realized separating；Component A is passed through into tower top
Condenser is condensed into liquid phase, enters back into the first phase-splitter split-phase, and the upper strata of the first phase-splitter is that ethyl acetate content is 94 ~ 96%
The ester phase of wt, lower floor is the water phase that water content is 90 ~ 92%wt；Ester mutually part extraction a, part is back to public rectifying in tower
Section, ester phase reflux ratio is 2.5-4；Water mutually part extraction a, part is back to public rectifying section in tower, and aqueous-phase reflux ratio is
0.4-0.65；And B component enters the top half of main column section；
（3）Described B, component C sequentially pass through public stripping section and the bottom of main column section is realized separating；Wherein component C enters public
The bottom of stripping section, produces from tower reactor altogether；And remaining B component is then into the latter half of main column section, and from main column section
Partial B component is converged in the middle part of main column section together, then sideline product extraction, and sideline product is condensed through side line condenser
Afterwards, the second phase-splitter split-phase is entered back into, the upper strata in the second phase-splitter is that n-butyl acetate content is the ester phase of 89 ~ 92%wt, under
Layer is the water phase that water content is 90 ~ 92%wt.
2. the method for reactive distillation next door tower coproduction ethyl acetate as claimed in claim 1 and n-butyl acetate, it is characterized by
Three kinds of feedstock temperature are 40-50 DEG C；The mole of feed ratio of ethanol and n-butanol is 3-4:1；Acetic acid rubs with ethanol
Your charge proportion is 1.2-2：1；The concentration of feed ethanol is 95%wt；Raw material butanol concentration is 100%wt；The concentration of raw acetic acid
It is 80%-100%wt.
3. the method for reactive distillation next door tower coproduction ethyl acetate as claimed in claim 1 and n-butyl acetate, it is characterized by
The number of theoretical plate of described prefractionation section is 20-40；The number of theoretical plate of public rectifying section is 5-15；The number of theoretical plate of main column section is
20-40；The number of theoretical plate of public stripping section is 5-15；Conversion zone is on prefractionation section 10-30 block theoretical plates.
4. the method for reactive distillation next door tower coproduction ethyl acetate as claimed in claim 1 and n-butyl acetate, it is characterized by
The feed entrance point of described feed ethanol is 10 ~ 20 pieces of theoretical plates of prefractionation section；Described raw material n-butanol and acetic acid enter
Material position is set to 15 ~ 30 blocks of column plates of prefractionation section；The extraction position of sideline product is the 10-25 block theoretical plates of main column section.
5. the method for reactive distillation next door tower coproduction ethyl acetate as claimed in claim 1 and n-butyl acetate, it is characterized by
Both sides of the decline liquid phase of public rectifying section at the top of dividing plate proportionally 0.48-2.3：1 is allocated, and respectively enters prefractionation
Section and main column section；Both sides proportionally 0.48-2.3 of the rising vapour phase of public stripping section in dividing plate bottom：1 is allocated, point
Jin Ru not prefractionation section and main column section.
6. the method for reactive distillation next door tower coproduction ethyl acetate as claimed in claim 1 and n-butyl acetate, it is characterized by
Described reactive distillation next door tower is packed tower.
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| CN108467744A (en) * | 2018-03-27 | 2018-08-31 | 天津大学 | A kind of the subtracting five line product method for upgrading of Lube Type decompression partitioned column |
| CN109663375A (en) * | 2017-10-13 | 2019-04-23 | 中国石油化工集团公司 | A kind of separation method of next door rectifying column and hydrocarbon mixture |
| CN112585112A (en) * | 2018-08-22 | 2021-03-30 | 伊士曼化工公司 | Process for the catalytic production of a purified enal product from an aldehyde feed stream using a single enclosed apparatus |
| CN113230685A (en) * | 2021-05-08 | 2021-08-10 | 北京化工大学 | Tower of two partition wall towers of two reaction section |
| CN113230682A (en) * | 2021-05-08 | 2021-08-10 | 北京化工大学 | Double-partition-wall reaction rectification structure and design method |
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