CN114394894B - Method and device for extracting Gao Chungeng acid from side line of vacuum batch distillation - Google Patents

Method and device for extracting Gao Chungeng acid from side line of vacuum batch distillation Download PDF

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CN114394894B
CN114394894B CN202210100163.1A CN202210100163A CN114394894B CN 114394894 B CN114394894 B CN 114394894B CN 202210100163 A CN202210100163 A CN 202210100163A CN 114394894 B CN114394894 B CN 114394894B
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tower
acid
batch
side line
chungeng
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CN114394894A (en
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王传昌
吴高胜
许保云
艾波
李瑜哲
包春凤
王世忠
刘陈真
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Shanghai Research Institute of Chemical Industry SRICI
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    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
    • C07C51/42—Separation; Purification; Stabilisation; Use of additives
    • C07C51/43—Separation; Purification; Stabilisation; Use of additives by change of the physical state, e.g. crystallisation
    • C07C51/44—Separation; Purification; Stabilisation; Use of additives by change of the physical state, e.g. crystallisation by distillation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/14—Fractional distillation or use of a fractionation or rectification column
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/14—Fractional distillation or use of a fractionation or rectification column
    • B01D3/32—Other features of fractionating columns ; Constructional details of fractionating columns not provided for in groups B01D3/16 - B01D3/30
    • B01D3/322—Reboiler specifications
    • 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
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Crystallography & Structural Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

The invention relates to a method and a device for extracting Gao Chungeng acid from a side line of vacuum batch distillation, which are characterized in that crude heptanoic acid raw materials are fed into a tower kettle of the batch distillation tower, first, total reflux operation is carried out, then, a part of light components, transition fractions and the rest are extracted by adopting a variable reflux ratio and reflux is carried out to the tower, then, secondary total reflux operation is carried out continuously, and then, a stream is extracted from the side line of the batch distillation tower, and cooled by a recooler, thus obtaining Gao Chungeng acid products. Compared with the prior art, the invention can obtain the high-purity heptanoic acid product with the mass fraction of more than 99.4 percent on the basis of reaching industrial productivity and large single-line operation range.

Description

Method and device for extracting Gao Chungeng acid from side line of vacuum batch distillation
Technical Field
The invention belongs to the technical field of Gao Chungeng acid rectification separation, and relates to a method and a device for extracting Gao Chungeng acid from a side line of vacuum batch rectification.
Background
Heptanoic acid, also known as glucuronic acid, has a boiling point of 223 ℃ and a melting point of-10.5 ℃ under normal pressure, is a colorless oily liquid, has a fatty smell, is impure and has malodor, is an important organic synthesis intermediate, and is used as a synthesis raw material for perfumes, medicines, lubricants and plasticizers, is slightly soluble in water, and is soluble in ethanol and diethyl ether. The synthesis process is that heptene-1 and synthesis gas are carbonylated to prepare heptaldehyde, and then air oxidation is carried out to obtain heptanoic acid. Firstly, feeding 1-heptene synthesis gas (carbon monoxide+hydrogen), recycle gas and catalyst solution into a carbonylation reactor, wherein the temperature is controlled to be 94-150 ℃ and the pressure is controlled to be 1.30MPa; the reaction product is subjected to reduced pressure flash evaporation to separate aldehydes, and the catalyst and the heavy components can be recycled. The aldehydes are then fed to a chemical book oxidation reactor where oxidation is carried out in air at a pressure of less than 0.69MPa in a mixed transition metal catalyst system. Wherein the aldehyde reaches almost the full conversion and therefore no separation and recycle is necessary. The obtained product is sent to a double-tower rectifying system after the micro catalyst is removed, heavy components (which can be used as fuel) are removed in a first tower, and the tower top material is sent to a second tower, thus obtaining the finished branched acid. Or by pyrolysis of castor oil or derivatives to produce heptanal, which is then oxidized to produce heptanoic acid.
During the synthesis reaction, some by-product impurities, such as caproic acid, caprylic acid, etc., may be produced. At present, the purity of heptanoic acid in the domestic market is generally about 98%, and a few can reach 99%, but the product quality is unstable. In some high-end downstream applications, the purity of the heptanoic acid is required to be high, the purity of the heptanoic acid must reach more than 99%, and the higher the content, the more expensive the heptanoic acid can reach the export standard. In the system of generating the heptanoic acid mixture by reaction, because of the existence of byproduct impurities such as light components, heavy components and the like, certain difficulty is brought to the purification of the heptanoic acid, and particularly, in the separation process, octanoic acid is always extracted along with the tower top product, so substances such as octanoic acid exist in the process of extracting the heptanoic acid from the tower top, thereby influencing the purity of the heptanoic acid. At present, most of the purification processes adopted by the heptanoic acid are ordinary vacuum batch rectification, and the heptanoic acid purity is not up to a very high level due to the existence of octanoic acid, so that the yield of the heptanoic acid can be reduced, and products with higher purity, such as heptanoic acid, and the like and higher in weight components, need to be returned into a tower again for secondary rectification, so that the energy consumption and the operation time are greatly increased.
Disclosure of Invention
The invention aims to provide a method and a device for extracting Gao Chungeng acid from a side line by vacuum batch distillation, which further improve the purity of heptanoic acid, reduce the content of octanoic acid impurities and the like.
The aim of the invention can be achieved by the following technical scheme:
according to the technical scheme, the method for extracting Gao Chungeng acid from the side line of the vacuum batch rectification is provided, a crude heptanoic acid raw material is sent to the tower kettle of the batch rectification tower, first, total reflux operation is carried out, then, a part of light components, transition fractions and the rest are extracted by adopting a variable reflux ratio and are refluxed into the tower, then, secondary total reflux operation is carried out continuously, and then, a stream is extracted from the side line of the batch rectification tower, and cooled by a recooler, so that Gao Chungeng acid products are obtained.
Further, the overhead operating pressure of the batch rectifying column is controlled to be 2 to 10kpa.a, preferably 2 to 5kpa.a, and the heating temperature of the column bottom is controlled to be 100 to 200 ℃, preferably 140 to 165 ℃.
Further, the overhead temperature at the time of one total reflux operation is maintained at 50 to 150 ℃, preferably 76.6 to 138 ℃, and the time of one total reflux is 1hr.
Further, the variable reflux ratio is varied in the range of 1:1 to 25:1, preferably 2:1 to 15:1.
Further, the extraction ratio of the light component to the transition fraction is 40-46%.
Further, the number of theoretical plates at the side line of the batch rectifying tower is 5-35 from top to bottom, preferably 5-15.
Further, the overhead temperature at the time of the secondary total reflux operation was 129 to 131℃for 1hr.
Further, in the side offtake, the overhead temperature of the batch rectifying column is maintained at 130 to 140 ℃, preferably 138 to 140 ℃, and the temperature at the side offtake position is maintained at 135 to 145 ℃, preferably 140 to 142 ℃.
Further, the refrigerant temperature of the recooler is-10 to 0 ℃, preferably-5 to 0 ℃.
Further, the crude heptanoic acid raw material comprises butyric acid, acetonitrile, valeric acid, caproic acid, heptanoic acid and caprylic acid.
Further, the batch rectifying tower is internally provided with a high-efficiency separation filler and a distributor, wherein the high-efficiency separation filler comprises plate corrugation, mesh grid filler, pulse filler, plate net, silk screen structured filler or high-efficiency structured filler, and the distributor comprises a tubular distributor, a trough plate distributor and the like.
Further, a batch rectifying tower reboiler adopts a conventional reboiler to provide steam; the condenser at the top of the batch rectifying tower adopts a normal-temperature water cooling mode, and the recooler adopts a low-temperature water or low-temperature glycol cooling mode.
Furthermore, the pipeline for fluid transportation adopts winding high-temperature heat tracing belt, heat-insulating cotton heat insulation or jacket steam heat insulation.
The second technical scheme of the invention provides a device for extracting Gao Chungeng acid from a side line of vacuum batch distillation, which is used for implementing the method, and comprises a batch distillation tower, a raw material tank, a reboiler, a circulating pump, a condenser, a recooler and a plurality of product tanks, wherein the raw material tank is connected with the bottom of the batch distillation tower through a feed pump, the reboiler is connected with the circulating pump in series and is connected with the bottom of the batch distillation tower to form circulation, a gas phase outlet of the top of the batch distillation tower is connected with the condenser, a condensate outlet of the condenser is led out of two branches, one branch is connected with at least one product tank, the other branch is connected with the top of the batch distillation tower in a return way, and the side line extraction branch is further arranged on the batch distillation tower and is sequentially connected with the recooler and the rest product tanks.
Compared with the prior art, the method can obtain the heptanoic acid high-purity product with the mass fraction of more than 99.4% on the basis of achieving large industrial productivity and single-line operation range by the side line extraction and product re-cooling device of the vacuum batch rectifying tower. Compared with the traditional process for producing heptanoic acid, the purity of the product is improved by 0.5-1.5%, the content of octanoic acid impurities in the product is reduced by 90-95%, the product can be sold as a high-end export product, the recovery rate of the product is improved by 10-15%, and the product has extremely high economic value. The process and the device have the advantages of stable process operation, stable product quality and high recovery rate.
Drawings
FIG. 1 is a flow chart of the process of purifying heptanoic acid according to the present invention;
FIG. 2 is a flow chart of a process for purifying heptanoic acid by batch distillation in comparative example 1;
the figure indicates:
v101-a raw material tank; v102-first product tank; v103-second product tank; v104-third product tank; p101-a feed pump; p102-a circulating pump; t101-a batch rectifying tower; e101-reboiler; e102-a condenser; e103-recooler.
Detailed Description
The invention will now be described in detail with reference to the drawings and specific examples. The present embodiment is implemented on the premise of the technical scheme of the present invention, and a detailed implementation manner and a specific operation process are given, but the protection scope of the present invention is not limited to the following examples.
In the following examples, the batch rectifying column used was filled with a high-efficiency separation packing and a distributor, wherein the high-efficiency separation packing was a wire mesh structured packing, and the distributor was a conventional trough-tray distributor. The remainder, unless specifically stated, is indicative of a conventional commercially available feedstock or conventional processing technique in the art.
Example 1
The flow chart of the method is shown in figure 1, and the raw materials of the crude heptanoic acid comprise 0.62wt% of butyric acid, 1.2wt% of acetonitrile, 0.2wt% of valeric acid, 18wt% of caproic acid, 76.1wt% of heptanoic acid and 3.88wt% of caprylic acid. The raw materials are conveyed from a raw material tank V101 to a tower kettle of a batch rectifying tower T101 at one time through a feed pump P101P101, cooling water is led into a condenser E102, a refrigerant is led into a recooler E103, the pressure of the top of the batch rectifying tower T101 is 2.25kPa. A, raw material liquid in the tower kettle circulates in the batch rectifying tower T101 through a circulating pump P102, the raw material liquid is heated through a reboiler E101, the heating temperature is 155 ℃, the circulating material is partially vaporized and rises to the top of the tower, heat transfer and mass transfer are carried out between the whole reflux tower and the rising vapor phase after the raw material liquid is condensed through the condenser E102, namely, the whole reflux is carried out at the beginning operation, the temperature of the top of the tower is stabilized at 75-75.5 ℃ for 1hr, the reflux ratio of the light component and the transition fraction is set to be 10:1, and 42% of light component and transition fraction are collected into a product tank V102. Then, the second total reflux is carried out, the temperature of the top of the tower is stabilized at 130-131 ℃ during the second total reflux, finally, the side line is extracted, the side line extraction position is 10 theoretical plates (from top to bottom), the side line extraction position is extracted, the extraction temperature is maintained at 136-142 ℃, the temperature of the top of the tower is controlled at 132-134 ℃, and then, the high-purity heptanoic acid is obtained by crystallizing the heavy components easy to crystallize such as octanoic acid and the like in the high-purity heptanoic acid through a recooler E103, and the heptanoic acid is sent into a second product tank V103 and a third product tank V104. After side stream extraction and recooler E103 recooler, the product heptanoic acid purity was over 99.47%, the recovery rate of acceptable product was 43%, the octanoic acid impurity content was less than 0.001% (no peak was detected by chromatography), and the single kettle operation time was 98hr.
Table 1 shows the results of chromatographic detection of the product of example 1
TABLE 1
Sequence number Name of the name Content/wt%
1 Paracoctanone(s) 0.0332
2 Valeric acid 0.3134
3 Caproic acid 0.1834
4 Heptanoic acid 99.47
Example 2
The flow chart of the process of the invention is also shown in FIG. 1, and the crude heptanoic acid raw material composition is 0.22wt% of butyric acid, 1.4wt% of acetonitrile, 0.1wt% of valeric acid, 16wt% of caproic acid, 78.1wt% of heptanoic acid and 3.98wt% of caprylic acid. Introducing a refrigerant to a sub-cooler E103, introducing a refrigerant to a temperature of-5 ℃, enabling the pressure at the top of a batch rectifying tower T101 to be 3.325kPa.A, heating to a temperature of 165 ℃, enabling the circulating material to be partially vaporized and raised to the top of the tower, condensing by a condenser E102, conducting heat transfer and mass transfer with the raised vapor phase in the whole reflux tower, namely conducting total reflux at the beginning of operation, stabilizing the temperature of the top of the tower at 76-76.8 ℃ during total reflux, fully refluxing for 1hr, then partially extracting, setting the reflux ratio of light components and transition fractions to be 8:1, extracting 45% of light components and transition fractions to enter a product tank V102, conducting secondary total reflux, stabilizing the temperature of the top of the tower at 129.8-131 ℃, finally, obtaining a side line extraction position of 12 theoretical plates at the position, maintaining the temperature of the top of the tower at 138-145 ℃, controlling the temperature of the top of the tower at 136-140 ℃, and crystallizing the iso-crystallizing heavy components in the tower through a sub-cooler E103 to obtain high-purity heptanoic acid. After side stream extraction and recooler E103 recooler, the product heptanoic acid purity was over 99.4%, the recovery rate of the qualified product was 41%, the octanoic acid impurity content was 0.05%, and the single kettle operation time was 95hr.
Example 3:
the flow chart of the method is shown in figure 1, and the raw materials of the crude heptanoic acid comprise 0.32wt% of butyric acid, 1.4wt% of acetonitrile, 0.1wt% of valeric acid, 15wt% of caproic acid, 79.1wt% of heptanoic acid and 3.88wt% of caprylic acid. Introducing a refrigerant into a recooler, introducing a refrigerant to 4 ℃, intermittently rectifying the pressure at the top of the tower at 3kPa. A, heating to 163 ℃, partially vaporizing and rising the circulating materials to the top of the tower, condensing the circulating materials by a condenser, then carrying out heat transfer and mass transfer with the rising vapor phase in the whole reflux tower, namely, carrying out total reflux at the beginning of operation, stabilizing the temperature of the top of the tower at 76.9-77.8 ℃, fully refluxing for 1hr, then partially extracting, setting the reflux ratio of light components and transitional fractions at 9:1, extracting 43% of light components and transitional fractions into a product tank 1, then carrying out secondary total reflux, stabilizing the temperature of the top of the tower at 129-131 ℃, finally extracting a side line at 9 theoretical plates (from top to bottom), maintaining the extracting temperature at 137-144 ℃, crystallizing the easily crystallized heavy components such as octanoic acid in the tower at 132-136 ℃ by the recooler, and obtaining high-purity heptanoic acid. After side stream extraction and recooler, the product heptanoic acid purity was 99.43% or higher, the recovery rate of the qualified product was 45%, the octanoic acid impurity content was 0.04%, and the single kettle operation time was 93hr.
Comparative example 1
Comparative example process scheme referring to fig. 2, the starting materials consisted of 0.4wt% butyric acid, 1.1wt% acetonitrile, 0.3wt% valeric acid, 14wt% caproic acid, 79.22wt% heptanoic acid and 4.98wt% caprylic acid, with the following optimum operating conditions: the raw materials are pumped into the tower kettle of the batch rectifying tower T101 through the feeding pump P101 at one time, the circulating pump P102 of the tower kettle circulates the material liquid, the material liquid is vaporized after being heated, vapor phase is extracted from the tower top to be condensed, part of condensate is refluxed, part of condensate is extracted, products are all extracted from the tower top, and the products are not extracted from the tower kettle. The batch distillation process is set to 3 stages, namely a light component stage, a transition fraction stage and a product stage. The operating parameters are the light component phases respectively: the pressure at the top of the tower is 3kPa. A, the reflux ratio is 3, and the theoretical plate number is 60; transition fraction stage: the pressure at the top of the tower is 3kPa. A, the reflux ratio is 10, and the theoretical plate number is 60; the production stage comprises the following steps: the column top pressure was 5kPa. A, the reflux ratio was 4, and the number of theoretical plates was 60. After batch rectification operation, the purity of the heptanoic acid product is 98.5%, the recovery rate of the qualified product is 30%, the content of octanoic acid impurity is 0.5%, and the single kettle operation time is 130hr.
The previous description of the embodiments is provided to facilitate a person of ordinary skill in the art in order to make and use the present invention. It will be apparent to those skilled in the art that various modifications can be readily made to these embodiments and the generic principles described herein may be applied to other embodiments without the use of the inventive faculty. Therefore, the present invention is not limited to the above-described embodiments, and those skilled in the art, based on the present disclosure, should make improvements and modifications without departing from the scope of the present invention.

Claims (3)

1. A method for extracting Gao Chungeng acid from a side line of vacuum batch rectification is characterized in that crude heptanoic acid raw material is fed into a tower kettle of a batch rectification tower, first, total reflux operation is carried out, then, a part of light components, transition fractions and the rest are extracted by adopting a variable reflux ratio and reflux into the tower, then, secondary total reflux operation is carried out continuously, and then, a stream is extracted from the side line of the batch rectification tower, and cooled by a recooler, thus obtaining Gao Chungeng acid products;
the operation pressure of the top of the batch rectifying tower is controlled to be 2-10kPa.A, and the heating temperature of the tower kettle is controlled to be 100-200 ℃;
the temperature of the tower top is maintained at 50-150 ℃ during one-time total reflux operation, and the time of one-time total reflux is 1hr;
the variable range of the variable reflux ratio is 1:1-25:1;
the extraction ratio of the light component to the transition fraction is 40-46%;
the number of theoretical plates extracted from the side line of the batch rectifying tower is 5-35 from top to bottom;
the temperature of the top of the tower is 129-131 ℃ and the time is 1hr during the secondary total reflux operation;
when the side line is extracted, the temperature of the top of the batch rectifying tower is maintained at 130-140 ℃, and the temperature of the side line extraction position is maintained at 135-145 ℃;
the crude heptanoic acid raw material comprises butyric acid, acetonitrile, valeric acid, caproic acid, heptanoic acid and caprylic acid.
2. The method for extracting Gao Chungeng acid from a vacuum batch distillation side stream as claimed in claim 1, wherein the temperature of the refrigerant in the recooler is-10-0 ℃.
3. The method for extracting Gao Chungeng acid from the side line of vacuum batch rectification according to claim 1 or 2, which is characterized in that the method is implemented on the basis of a device for extracting Gao Chungeng acid from the side line of vacuum batch rectification, the device comprises a batch rectification tower, a raw material tank, a reboiler, a circulating pump, a condenser, a recooler and a plurality of product tanks, wherein the raw material tank is connected with the bottom of the batch rectification tower through a feed pump, the reboiler is connected with the circulating pump in series and is connected with the bottom of the batch rectification tower to form circulation, a gas phase outlet at the top of the batch rectification tower is connected with the condenser, a condensate outlet of the condenser is led out into two branches, one branch is connected with at least one product tank, the other branch is connected with the top of the batch rectification tower in a returning way, and the side line extraction branch is further arranged on the batch rectification tower and is sequentially connected with the recooler and the rest product tanks.
CN202210100163.1A 2022-01-27 2022-01-27 Method and device for extracting Gao Chungeng acid from side line of vacuum batch distillation Active CN114394894B (en)

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Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102329186A (en) * 2011-07-25 2012-01-25 天津市泰旭物流有限公司 Method for preparing high-purity 1,2-butadiene by batch rectification method of ice water condensation
CN105418430A (en) * 2015-12-16 2016-03-23 东营市海科新源化工有限责任公司 Device and method for preparing high-purity dimethyl carbonate through batch rectification
CN110642708A (en) * 2019-10-31 2020-01-03 中国农业科学院农业环境与可持续发展研究所 Method for separating and extracting caproic acid, heptanoic acid and octanoic acid from livestock and poultry manure anaerobic acidification liquid

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102329186A (en) * 2011-07-25 2012-01-25 天津市泰旭物流有限公司 Method for preparing high-purity 1,2-butadiene by batch rectification method of ice water condensation
CN105418430A (en) * 2015-12-16 2016-03-23 东营市海科新源化工有限责任公司 Device and method for preparing high-purity dimethyl carbonate through batch rectification
CN110642708A (en) * 2019-10-31 2020-01-03 中国农业科学院农业环境与可持续发展研究所 Method for separating and extracting caproic acid, heptanoic acid and octanoic acid from livestock and poultry manure anaerobic acidification liquid

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