CN105194895A - Thermal coupling partition wall reactive distillation column for preparing biodiesel and method for producing biodiesel - Google Patents
Thermal coupling partition wall reactive distillation column for preparing biodiesel and method for producing biodiesel Download PDFInfo
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- CN105194895A CN105194895A CN201510553668.3A CN201510553668A CN105194895A CN 105194895 A CN105194895 A CN 105194895A CN 201510553668 A CN201510553668 A CN 201510553668A CN 105194895 A CN105194895 A CN 105194895A
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/10—Biofuels, e.g. bio-diesel
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
Abstract
The invention discloses a thermal coupling partition wall reactive distillation column for preparing biodiesel and a method for producing biodiesel. The thermal coupling partition wall reactive distillation column comprises a condenser, a reboiler and a main column body provided with a partition wall, wherein the main column body comprises a reaction separation area, an extraction area and a column bottom area. The method for preparing high-purity biodiesel comprises the steps that raw oil and alcohol are preheated and then enter the reaction separation area to make contact with a catalyst for reaction predissociation, the by-product water is extracted through the top of the reaction separation area, the target product high-purity biodiesel is extracted through the column bottom area and provides energy required by preheating of raw materials, and the unreacted alcohol is extracted through the top of the extraction area. According to the method, reaction and separation of the three substances are integrated in one column, and the effect of two distillation columns is realized through one distillation column. Compared with the conventional technology, the thermal coupling partition wall reactive distillation column has the advantages that equipment investment is reduced, energy consumption is reduced, and high-purity biodiesel can be produced.
Description
Technical field
The present invention relates to technical field of biochemical industry, particularly relate to a kind of thermal coupling next door reactive distillation column for the preparation of biodiesel and production method thereof.
Background technology
Biodiesel (BiodieselFuel) is the long-chain mono alkyl ester made for feedstock oil with vegetable oil or animal tallow etc., the reproducibility diesel fuel that petrifaction diesel is used in compression ignition engine can be replaced, compared with traditional fossil energy, its sulphur and arene content is low, flash-point is high, Cetane number is high, have good lubricity, can partly add in petrifaction diesel.
In recent years, along with the day by day exhausted of fossil energy and the mankind's sharply riseing to fuel energy demand, Biodiesel is in widespread attention.Can improve energy net gain, whether there is environmental benefit and economic competitiveness, and to produce in a large number under the prerequisite not reducing staple food supply be the prerequisite that can biodiesel realize commercial Application.In production biodiesel process, catalyst plays a part key, and conventional has base catalyst, acidic catalyst, enzyme catalyst and organic catalyst etc.
Biological enzyme production biodiesel has reaction condition gentleness, the advantages such as energy consumption is low, low for equipment requirements.Patent CN1436834A provides a kind of method of short-chain aliphatic ester synthesising biological oil plant, at suitable temperature, utilize the renewable resource production biodiesel such as biological enzyme animal and plant fat.But biological enzyme production cost is high, reaction efficiency is low, and catalyzing enzyme easy in inactivation, which prevent the application in the industrial production of biological enzyme technology, be now in the exploratory stage to its research.
Compared with biological enzyme biodiesel synthesis, chemical method production biodiesel has that production cost is lower, reaction easily controls, grease conversion ratio advantages of higher, and for enhancing productivity, to reduce production cost significant.Patent CN103756791A utilizes waste grease, production biodiesel under the effect of composite catalyst, and grease conversion ratio is higher, catalyst reusable edible.Patent CN103756792A removes most of free fatty in degrease by pretreatment and effectively reduces water content, the soap in biodiesel, glycerine, part foreign pigment etc. are effectively removed by atlapulgite process in ester exchange, and stabilizing agent is added in post processing, add the stability of biodiesel.
Although chemical method can improve the conversion ratio of bio-oil, reduce production cost, its higher energy consumption load also becomes method one of extensive use problems faced in the industry for this reason.Domestic and international experts and scholars, at reduction plant energy consumption, reduce operating cost aspect and have made outstanding contribution.Patent CN103320233A proposes a kind of method utilizing continuous tubular reactor production biodiesel, the method esterification reaction process does not heat, does not stir, energy-efficient, and whole flow process is carried out under low-temperature atmosphere-pressure environment, energy ezpenditure is low, utilization rate is high, energy-conserving and environment-protective; Patent US2008312460A1 develops a kind of Vltrasonic device, utilizes multi-frequency ultrasonic energy, and vegetable oil or animal oil are converted into biodiesel, saves energy consumption.
Summary of the invention
Produce energy consumption this problem higher in biodiesel process for reducing chemical method, the present invention proposes a kind of by utilizing reactive distillation column production biodiesel in thermal coupling next door to reduce the high-purity biodiesel preparation method that equipment investment reduces energy consumption.
The object of this invention is to provide a kind of process and the device of producing high-purity biodiesel.Traditional two-tower process is reduced to single tower flow process by utilizing thermal coupling next door reactive distillation column by the present invention, decrease equipment investment, and utilize thermal coupling in tower to reduce the energy consumption of production of biodiesel, in addition afterwards high-temperature product at the bottom of tower is used for raw material preheating, improves energy utilization efficiency significantly.
The present invention adopts following technical scheme:
The present invention comprises king-tower, the overhead water condenser with partition wall, tower top alcohol condenser and tower bottom reboiler for the preparation of the thermal coupling next door reactive distillation column of biodiesel; King-tower inside is divided into Reaction Separation region, extraction region and territory, tower base area, territory, tower base area is positioned at rectifying column bottom, Reaction Separation region and extraction region are positioned at the middle and upper part of rectifying column, both are come by vertical baffle for separating, vertical clapboard upper end is connected with rectifying column tower top, and lower end overlying regions at the bottom of tower is unsettled.
The rectifying column outside in Reaction Separation region is connected with feedstock oil feed pipe and raw alcohol feed pipe, two pipelines is respectively equipped with fuel oil preheating device and raw alcohol preheater; Overhead water condenser is by the tower top of pipeline coupled reaction separated region; Tower top alcohol condenser connects the tower top in extraction region by pipeline; Be provided with discharge nozzle at the bottom of the tower of rectifying column, discharge nozzle is divided into two, and a rectifying tower body connecting tower bottom reboiler and connect extraction region again, another root connects fuel oil preheating device and raw alcohol preheater successively.
Described Reaction Separation area filling catalysts, plays reactive distillation effect, and area filling High Efficient Standard Packing or column plate at the bottom of extraction region and tower, play rectifying centrifugation.
The method utilizing thermal coupling next door of the present invention reactive distillation column to prepare biodiesel is:
Feedstock oil and alcohol after preheating, enter Reaction Separation region and catalyst exposure carries out reaction pre-separation, water byproduct is flowed out by top, Reaction Separation region, target product high-purity biodiesel component is flowed out by territory, tower base area and preheating institute energy requirement of supplying raw materials, and unreacted component methyl alcohol is via the top extraction of extraction region.
Described feedstock oil is free fatty.
Described raw alcohol is monohydric alcohol, is preferably methyl alcohol.
Described catalyst is solid phase acid catalyst.
Thermal coupling next door reactive distillation column operating pressure is 100 ~ 1000kPa, reaction zone tower top operating temperature is 117 ~ 152 DEG C, Reaction Separation region (I) operating temperature is 102 ~ 145 DEG C, and territory, tower base area (III) operating temperature is 120 ~ 350 DEG C.
Concrete steps are as follows:
Raw alcohol enters thermal coupling next door reactive distillation column by bottom, Reaction Separation region after preheating, feedstock oil enters thermal coupling next door reactive distillation column by Reaction Separation area top after preheating, there is esterification in two raw materials, generate target product biodiesel and water byproduct under the effect of solid acid catalyst.Be separated at the Reaction Separation region byproduct of reaction water of thermal coupling next door reactive distillation column, obtain highly purified water at tower top, by the extraction of overhead condenser condensation rear portion, another part returns in tower as overhead reflux.Be separated in territory, the tower base area high boiling component biodiesel of thermal coupling next door reactive distillation column, and at the bottom of tower, obtain highly purified biodiesel, the biodiesel that temperature reduces after tower bottom reboiler heat exchange rear portion carries out heat exchange as the thermal source of feeding preheating by feed preheater is as product extraction, and another part returns in tower as the rising steam that refluxes at the bottom of tower.Be separated at the extraction region unreacted components methyl alcohol of thermal coupling next door reactive distillation column, and obtain highly purified methyl alcohol at tower top, by the extraction of tower top alcohol condenser condenses rear portion, another part returns in tower as overhead reflux.
Relative to prior art, effect of the present invention is:
In the reactive distillation column of thermal coupling next door, realize the production of high-purity biodiesel, the multitower of traditional reactive distillation and later separation purifying technique is incorporated in a thermal coupling next door reactive distillation column, saves equipment investment, reduce energy consumption.Thermal coupling next door reactive distillation tower process realizes closed cycle, and the raw material backflow recycling of non-complete reaction, improves total conversion.
The feed side of next door rectifying column of the present invention fills catalysts, reaction is carried out in pre-separation section, namely constitutes thermal coupling next door reactive distillation column.By this technique, feedstock oil conversion ratio is more than 99%, and gained biodiesel purity, more than 99.5%, reaches same percent hydrolysis and separation of products requirement, can save energy more than 30% than popular response distillation process.
Accompanying drawing explanation
Fig. 1 is the process flow diagram of thermal coupling next door reactive distillation column production high-purity biodiesel;
Description of reference numerals:
E1 overhead water condenser; E2 tower bottom reboiler; E3 tower top alcohol condenser; E4 fuel oil preheating device; E5 raw alcohol preheater; RDWC thermal coupling next door reactive distillation column king-tower; 1 feedstock oil; Feedstock oil after 2 preheatings; 3 raw alcohols; Raw alcohol after 4 preheatings; 5 Reaction Separation district overhead vapor stream; 6 extraction district tower top methanol steams; 7 condensed water; 8 condensed methyl alcohol; 9 Reaction Separation district overhead refluxes; 10 extraction district overhead refluxes; 11 return tower section biodiesel; 12 return tower biodiesel steam; 13 extraction part biological diesel oil; 14 with raw alcohol heat exchange after biodiesel oil product; 15 with feedstock oil heat exchange after biodiesel oil product; I Reaction Separation region; II extraction region; III territory, tower base area.
Detailed description of the invention
Below in conjunction with accompanying drawing, the specific embodiment of the present invention is described in detail.Should be understood that, detailed description of the invention described herein, only for instruction and explanation of the present invention, is not limited to the present invention.
As shown in Figure 1: the thermal coupling next door reactive distillation column for the preparation of biodiesel of the present invention comprises king-tower RDWC, the overhead water condenser E1 with partition wall, tower top alcohol condenser E3 and tower bottom reboiler E2; King-tower inside is divided into Reaction Separation region I, extraction region II and territory, tower base area III, territory, tower base area III is positioned at rectifying column bottom, Reaction Separation region I and extraction region II are positioned at the middle and upper part of rectifying column, both are come by vertical baffle for separating, vertical clapboard upper end is connected with rectifying column tower top, and lower end is unsettled above territory, tower base area III.
The rectifying column outside in Reaction Separation region I is connected with feedstock oil feed pipe and raw alcohol feed pipe, two pipelines is respectively equipped with fuel oil preheating device E4 and raw alcohol preheater E5; Overhead water condenser E1 is by the tower top of pipeline coupled reaction separated region I; Tower top alcohol condenser E3 connects the tower top in extraction region II by pipeline; Be provided with discharge nozzle at the bottom of the tower of rectifying column, discharge nozzle is divided into two, and a rectifying tower body connecting tower bottom reboiler E2 and connect extraction region II again, another root connects fuel oil preheating device E4 and raw alcohol preheater E5 successively.
Catalysts is filled in described Reaction Separation region I, plays reactive distillation effect, and High Efficient Standard Packing or column plate are filled in extraction region II and territory, tower base area III, play rectifying centrifugation.
The present invention adopts thermal coupling next door reactive distillation process flow process to be that raw alcohol enters thermal coupling next door reactive distillation column RDWC by bottom, Reaction Separation region after preheating, feedstock oil enters thermal coupling next door reactive distillation column RDWC by top, Reaction Separation region I after preheating, there is esterification in two raw materials, generate target product biodiesel and water byproduct under the effect of solid acid catalyst.Be separated at the Reaction Separation region I byproduct of reaction water of thermal coupling next door reactive distillation column RDWC, obtain highly purified water at tower top, by the extraction of overhead condenser E1 condensation rear portion, another part returns in tower as overhead reflux.Be separated in territory, the tower base area high boiling component biodiesel in thermal coupling next door reactive distillation column (RDWC), and at the bottom of tower, obtain highly purified biodiesel, the biodiesel that after a part of thermal source as feeding preheating carries out heat exchange by feed preheater E4 and E5, temperature reduces is as product extraction, and another part returns in tower as the rising steam that refluxes at the bottom of tower after tower bottom reboiler E2 heat exchange.Be separated at the extraction region II unreacted components methyl alcohol of thermal coupling next door reactive distillation column RDWC, and obtain highly purified methyl alcohol at tower top, by the extraction of overhead condenser E3 condensation rear portion, another part returns in tower as overhead reflux.
In order to production effect of the present invention is described better, choose three examples and be illustrated, these examples only for illustrative purposes, and are not intended to limit the scope of the invention.
Example 1:
The present invention adopts thermal coupling next door reactive distillation process flow process to be that raw alcohol enters thermal coupling next door reactive distillation column RDWC by bottom, Reaction Separation region after preheating, feedstock oil enters thermal coupling next door reactive distillation column RDWC by top, Reaction Separation region I after preheating, there is esterification in two raw materials, generate target product biodiesel and water byproduct under the effect of solid acid catalyst.Be separated at the Reaction Separation region I byproduct of reaction water of thermal coupling next door reactive distillation column RDWC, obtain highly purified water at tower top, by the extraction of overhead condenser E1 condensation rear portion, another part returns in tower as overhead reflux.Be separated in territory, the tower base area high boiling component biodiesel in thermal coupling next door reactive distillation column (RDWC), and at the bottom of tower, obtain highly purified biodiesel, the biodiesel that after a part of thermal source as feeding preheating carries out heat exchange by feed preheater E4 and E5, temperature reduces is as product extraction, and another part returns in tower as the rising steam that refluxes at the bottom of tower after tower bottom reboiler E2 heat exchange.Be separated at the extraction region II unreacted components methyl alcohol of thermal coupling next door reactive distillation column RDWC, and obtain highly purified methyl alcohol at tower top, by the extraction of overhead condenser E3 condensation rear portion, another part returns in tower as overhead reflux.
Flow process as shown in Figure 1.Each region actual plate number is as shown in table 1, feed rate and composition as shown in table 2.The feed entrance point (counting from top to bottom) of feedstock oil and alcohol is respectively thermal coupling next door reactive distillation column RDWC the 3rd piece and the 22nd piece of theoretical plate, and feeding temperature is 100 DEG C.Thermal coupling next door reactive distillation column RDWC operating pressure is 350kPa, and Reaction Separation region overhead extraction amount is 100kmol/h, and head temperature is 138 DEG C, and bottom temp is 107 DEG C; Extraction region overhead extraction amount is 100kmol/h, and head temperature is 99 DEG C, and bottom temp is 104 DEG C; Zone flow at the bottom of tower is 100kmol/h, and head temperature is 107 DEG C, and bottom temp is 339 DEG C.Each logistics flux and composition as shown in table 2, gained biodiesel purity is 99.99%.
Table 1 each region actual plate number
| Tower section | Reactive distillation region | Extraction region | Territory, tower base area |
| Actual plate number | 24 | 24 | 6 |
Table 2 example 1 each logistics quality flow and each constituent mass mark
Example 2:
The present invention adopts thermal coupling next door reactive distillation process flow process to be that raw alcohol enters thermal coupling next door reactive distillation column RDWC by bottom, Reaction Separation region after preheating, feedstock oil enters thermal coupling next door reactive distillation column RDWC by top, Reaction Separation region I after preheating, there is esterification in two raw materials, generate target product biodiesel and water byproduct under the effect of solid acid catalyst.Be separated at the Reaction Separation region I byproduct of reaction water of thermal coupling next door reactive distillation column RDWC, obtain highly purified water at tower top, by the extraction of overhead condenser E1 condensation rear portion, another part returns in tower as overhead reflux.Be separated in territory, the tower base area high boiling component biodiesel in thermal coupling next door reactive distillation column (RDWC), and at the bottom of tower, obtain highly purified biodiesel, the biodiesel that after a part of thermal source as feeding preheating carries out heat exchange by feed preheater E4 and E5, temperature reduces is as product extraction, and another part returns in tower as the rising steam that refluxes at the bottom of tower after tower bottom reboiler E2 heat exchange.Be separated at the extraction region II unreacted components methyl alcohol of thermal coupling next door reactive distillation column RDWC, and obtain highly purified methyl alcohol at tower top, by the extraction of overhead condenser E3 condensation rear portion, another part returns in tower as overhead reflux.
Flow process as shown in Figure 1.Each region actual plate number is as shown in table 3, feed rate and composition as shown in table 4.The feed entrance point (counting from top to bottom) of feedstock oil and alcohol is respectively thermal coupling next door reactive distillation column RDWC the 3rd piece and the 22nd piece of theoretical plate, and feeding temperature is 100 DEG C.Thermal coupling next door reactive distillation column RDWC operating pressure is 350kPa, and Reaction Separation region overhead extraction amount is 80kmol/h, and head temperature is 139 DEG C, and bottom temp is 107 DEG C; Extraction region overhead extraction amount is 80kmol/h, and head temperature is 100 DEG C, and bottom temp is 105 DEG C; Zone flow at the bottom of tower is 80kmol/h, and head temperature is 107 DEG C, and bottom temp is 339 DEG C.Each logistics flux and composition as shown in table 2, gained biodiesel purity is 99.99%.
Table 3 each region actual plate number
| Tower section | Reactive distillation region | Extraction region | Territory, tower base area |
| Actual plate number | 24 | 24 | 6 |
Table 4 example 1 each logistics quality flow and each constituent mass mark
Example 3:
The present invention adopts thermal coupling next door reactive distillation process flow process to be that raw alcohol enters thermal coupling next door reactive distillation column RDWC by bottom, Reaction Separation region after preheating, feedstock oil enters thermal coupling next door reactive distillation column RDWC by top, Reaction Separation region I after preheating, there is esterification in two raw materials, generate target product biodiesel and water byproduct under the effect of solid acid catalyst.Be separated at the Reaction Separation region I byproduct of reaction water of thermal coupling next door reactive distillation column RDWC, obtain highly purified water at tower top, by the extraction of overhead condenser E1 condensation rear portion, another part returns in tower as overhead reflux.Be separated in territory, the tower base area high boiling component biodiesel in thermal coupling next door reactive distillation column (RDWC), and at the bottom of tower, obtain highly purified biodiesel, the biodiesel that after a part of thermal source as feeding preheating carries out heat exchange by feed preheater E4 and E5, temperature reduces is as product extraction, and another part returns in tower as the rising steam that refluxes at the bottom of tower after tower bottom reboiler E2 heat exchange.Be separated at the extraction region II unreacted components methyl alcohol of thermal coupling next door reactive distillation column RDWC, and obtain highly purified methyl alcohol at tower top, by the extraction of overhead condenser E3 condensation rear portion, another part returns in tower as overhead reflux.
Flow process as shown in Figure 1.Each region actual plate number is as shown in table 5, feed rate and composition as shown in table 6.The feed entrance point (counting from top to bottom) of feedstock oil and alcohol is respectively thermal coupling next door reactive distillation column RDWC the 3rd piece and the 22nd piece of theoretical plate, and feeding temperature is 100 DEG C.Thermal coupling next door reactive distillation column RDWC operating pressure is 350kPa, and Reaction Separation region overhead extraction amount is 90kmol/h, and head temperature is 139 DEG C, and bottom temp is 107 DEG C; Extraction region overhead extraction amount is 90kmol/h, and head temperature is 99 DEG C, and bottom temp is 105 DEG C; Zone flow at the bottom of tower is 90kmol/h, and head temperature is 106 DEG C, and bottom temp is 339 DEG C.Each logistics flux and composition as shown in table 2, gained biodiesel purity is 99.99%.
Table 5 each region actual plate number
| Tower section | Reactive distillation region | Extraction region | Territory, tower base area |
| Actual plate number | 24 | 24 | 6 |
Table 6 example 1 each logistics quality flow and each constituent mass mark
Although illustrate and describe embodiments of the invention, for the ordinary skill in the art, be appreciated that and can carry out multiple change, amendment, replacement and modification to these embodiments without departing from the principles and spirit of the present invention, scope of the present invention is by claims and equivalents thereof.
Claims (10)
1. the thermal coupling next door reactive distillation column for the preparation of biodiesel, it is characterized in that: described rectifying column comprises king-tower (RDWC), the overhead water condenser (E1) with partition wall, tower top alcohol condenser (E3) and tower bottom reboiler (E2); King-tower inside is divided into Reaction Separation region (I), extraction region (II) and territory, tower base area (III), territory, tower base area (III) is positioned at rectifying column bottom, Reaction Separation region (I) and extraction region (II) are positioned at the middle and upper part of rectifying column, both are come by vertical baffle for separating, vertical clapboard upper end is connected with rectifying column tower top, and lower end is unsettled in top, territory, tower base area (III).
2. as claim 1 the thermal coupling next door reactive distillation column for the preparation of biodiesel, it is characterized in that: the rectifying column outside of Reaction Separation region (I) is connected with feedstock oil feed pipe and raw alcohol feed pipe, two pipelines are respectively equipped with fuel oil preheating device (E4) and raw alcohol preheater (E5); Overhead water condenser (E1) is by the tower top of pipeline coupled reaction separated region (I); Tower top alcohol condenser (E3) connects the tower top in extraction region (II) by pipeline; Discharge nozzle is provided with at the bottom of the tower of rectifying column, discharge nozzle is divided into two, a rectifying tower body connecting tower bottom reboiler (E2) and connect extraction region (II) again, another root connects fuel oil preheating device (E4) and raw alcohol preheater (E5) successively.
3. as claim 1 the thermal coupling next door reactive distillation column for the preparation of biodiesel, it is characterized in that: described Reaction Separation region (I) fills catalysts, play reactive distillation effect, High Efficient Standard Packing or column plate are filled in extraction region (II) and territory, tower base area (III), play rectifying centrifugation.
4. utilize the thermal coupling next door reactive distillation column as described in any one of claim 1-3 to prepare a method for biodiesel, it is characterized in that: the concrete steps of described method are as follows:
Feedstock oil and alcohol enter Reaction Separation region (I) and carry out reaction pre-separation with catalyst exposure after preheating, water byproduct is flowed out by Reaction Separation region (I) top, target product high-purity biodiesel component is flowed out by territory, tower base area (III) and preheating institute energy requirement of supplying raw materials, and unreacted component methyl alcohol is via extraction region (II) top extraction.
5. preparation method as claimed in claim 4, is characterized in that: described feedstock oil is free fatty.
6. preparation method as claimed in claim 4, is characterized in that: described raw alcohol is monohydric alcohol.
7. preparation method as claimed in claim 6, is characterized in that: described raw alcohol is methyl alcohol.
8. preparation method as claimed in claim 4, is characterized in that: described catalyst is solid phase acid catalyst.
9. preparation method as claimed in claim 4, it is characterized in that: thermal coupling next door reactive distillation column operating pressure is 100 ~ 1000kPa, reaction zone tower top operating temperature is 117 ~ 152 DEG C, Reaction Separation region (I) operating temperature is 102 ~ 145 DEG C, and territory, tower base area (III) operating temperature is 120 ~ 350 DEG C.
10. the thermal coupling next door reactive distillation column as described in any one of claim 1-3 is for the preparation of the application of biodiesel.
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| CN106823434A (en) * | 2017-01-06 | 2017-06-13 | 绍兴市上虞区耕创化工技术服务部 | Continous way double tower distilling apparatus and distillating method |
| CN107398090A (en) * | 2016-05-21 | 2017-11-28 | 中国石油化工股份有限公司 | A kind of method of spliced central dividing plate and transformation tradition rectifying column |
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| KR101165371B1 (en) * | 2009-03-19 | 2012-07-12 | 주식회사 엘지화학 | Dividing wall column for production of high purity acrylic acid and distillating method using thereof |
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| CN107398090A (en) * | 2016-05-21 | 2017-11-28 | 中国石油化工股份有限公司 | A kind of method of spliced central dividing plate and transformation tradition rectifying column |
| CN107398090B (en) * | 2016-05-21 | 2019-06-14 | 中国石油化工股份有限公司 | A kind of method of spliced intermediate bulkhead and bulkhead type rectification column and the traditional rectifying column of transformation |
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