CN110903184A - Apparatus for producing methacrylic acid - Google Patents

Apparatus for producing methacrylic acid Download PDF

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CN110903184A
CN110903184A CN201911069670.8A CN201911069670A CN110903184A CN 110903184 A CN110903184 A CN 110903184A CN 201911069670 A CN201911069670 A CN 201911069670A CN 110903184 A CN110903184 A CN 110903184A
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line
reactor
methacrolein
methacrylic acid
gas outlet
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须安范明
犬饲正二
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Sumitomo Chemical Co Ltd
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Sumitomo Chemical Co Ltd
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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
    • C07C51/16—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation
    • C07C51/21—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen
    • C07C51/23—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of oxygen-containing groups to carboxyl groups
    • C07C51/235—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of oxygen-containing groups to carboxyl groups of —CHO groups or primary alcohol groups
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
    • C07C51/16—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation
    • C07C51/21—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen
    • C07C51/25—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of unsaturated compounds containing no six-membered aromatic ring
    • C07C51/252—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of unsaturated compounds containing no six-membered aromatic ring of propene, butenes, acrolein or methacrolein
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/0046—Sequential or parallel reactions, e.g. for the synthesis of polypeptides or polynucleotides; Apparatus and devices for combinatorial chemistry or for making molecular arrays
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/0053—Details of the reactor
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C45/00—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds
    • C07C45/27—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation
    • C07C45/32—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen
    • C07C45/33—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen of CHx-moieties
    • C07C45/34—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen of CHx-moieties in unsaturated compounds
    • C07C45/35—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen of CHx-moieties in unsaturated compounds in propene or isobutene
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C45/00—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds
    • C07C45/27—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation
    • C07C45/32—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen
    • C07C45/37—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen of >C—O—functional groups to >C=O groups
    • C07C45/38—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen of >C—O—functional groups to >C=O groups being a primary hydroxyl group
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C45/00—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds
    • C07C45/27—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation
    • C07C45/32—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen
    • C07C45/37—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen of >C—O—functional groups to >C=O groups
    • C07C45/39—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen of >C—O—functional groups to >C=O groups being a secondary hydroxyl group
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C47/00—Compounds having —CHO groups
    • C07C47/20—Unsaturated compounds having —CHO groups bound to acyclic carbon atoms
    • C07C47/21—Unsaturated compounds having —CHO groups bound to acyclic carbon atoms with only carbon-to-carbon double bonds as unsaturation
    • C07C47/22—Acryaldehyde; Methacryaldehyde
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C57/00—Unsaturated compounds having carboxyl groups bound to acyclic carbon atoms
    • C07C57/02—Unsaturated compounds having carboxyl groups bound to acyclic carbon atoms with only carbon-to-carbon double bonds as unsaturation
    • C07C57/03—Monocarboxylic acids
    • C07C57/04—Acrylic acid; Methacrylic acid
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00274—Sequential or parallel reactions; Apparatus and devices for combinatorial chemistry or for making arrays; Chemical library technology
    • B01J2219/00277—Apparatus
    • B01J2219/00279—Features relating to reactor vessels
    • B01J2219/00331—Details of the reactor vessels
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00274—Sequential or parallel reactions; Apparatus and devices for combinatorial chemistry or for making arrays; Chemical library technology
    • B01J2219/00277—Apparatus
    • B01J2219/00351—Means for dispensing and evacuation of reagents
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00274—Sequential or parallel reactions; Apparatus and devices for combinatorial chemistry or for making arrays; Chemical library technology
    • B01J2219/00277—Apparatus
    • B01J2219/00495—Means for heating or cooling the reaction vessels

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

Abstract

The invention provides a methacrylic acid production apparatus having excellent continuous operability. A methacrylic acid production apparatus (100) comprising: a first reactor (10) for obtaining methacrolein; a second reactor (20) for obtaining methacrylic acid; a methacrolein recovery unit (70); a Line (LA) connecting the outlet (10j) of the first reactor (10) and the inlet (20i) of the second reactor (20); a Line (LB) connecting the Line (LA) and the oxygen supply source; a Line (LC) connecting the outlet (20j) of the second reactor 20 and the liquid inlet (70i) of the methacrolein recovery unit (70); and a Line (LD) connecting the gas outlet (70gj) of the methacrolein recovery unit (70) and the Line (LA), wherein the Line (LD) has a heating unit (23a), and the heating unit (23a) is disposed on at least a part of the line between the gas outlet (70gj) and a position where the line length is 30, when the line length from the gas outlet (70gj) to the connection portion (Xo) with the Line (LA) is set to 100.

Description

Apparatus for producing methacrylic acid
Technical Field
The present invention relates to a methacrylic acid production apparatus.
Background
Patent document 1 describes a method for producing methacrylic acid.
Documents of the prior art
Patent document
Patent document 1: international publication No. 2008/145417
Disclosure of Invention
Problems to be solved by the invention
A production apparatus used for producing methacrylic acid is required to be capable of continuous operation over a long period of time. Accordingly, an object of the present invention is to provide a methacrylic acid production apparatus having excellent continuous operability.
Means for solving the problems
The apparatus for producing methacrylic acid of the present invention comprises: a first reactor having an inlet and an outlet and for obtaining methacrolein from isobutylene and/or tert-butanol (hereinafter referred to as "TBA") and oxygen; a second reactor having an inlet and an outlet and for obtaining methacrylic acid by reacting methacrolein and oxygen; a methacrolein recovery unit having a liquid inlet, a liquid outlet, and a gas outlet; a line LA connecting the outlet of the first reactor and the inlet of the second reactor; a line LB connecting line LA and an oxygen supply; a line LC connecting an outlet of the second reactor and a liquid inlet of the methacrolein recovery unit; and a line LD connecting the gas outlet of the methacrolein recovery unit and the line LA, wherein the line LD has a heating unit, and the heating unit is disposed on at least a part of the line between the gas outlet and a position where the line length is 30, when the line length from the gas outlet to the connection Xo with the line LA is 100.
Such a methacrylic acid production apparatus is excellent in continuous operability.
The heating unit may be disposed in at least a part of a line extending from the gas outlet to a position where the length of the line is 20, or may be disposed in at least a part of a line extending from the gas outlet to a position where the length of the line is 10. This further improves the continuous operation performance.
The length of a line from the gas outlet to the inlet of the heating unit may be 3m or less. This further improves the continuous operation performance.
Effects of the invention
According to the present invention, a methacrylic acid production apparatus having excellent continuous operability can be provided.
Drawings
Fig. 1 is a diagram showing an example of an apparatus for producing methacrylic acid according to the present embodiment.
Reference numerals
10 … a first reactor,
20 … second reactor,
50b … gas mixer,
60 … liquefaction unit,
70 … methyl acrolein recovery unit,
23a … heating unit
100 … apparatus for producing methacrylic acid
Detailed Description
In the present specification, isobutylene means 2-methylpropene.
First, an apparatus 100 for producing methacrylic acid according to the present embodiment will be described with reference to fig. 1. Fig. 1 is a diagram showing an example of an apparatus for producing methacrylic acid according to the present embodiment.
The manufacturing apparatus 100 mainly includes: a first reactor 10, a second reactor 20, a liquefaction unit 60, a methacrolein recovery unit 70, and lines LA, LB, LC, and LD. Line LA has a gas mixer 50 b. Line LB has a compressor 55. The line LD has a heating unit 23 a.
A supply source (S0) of a gas containing isobutylene and/or TBA and oxygen is connected to the inlet 10i of the first reactor 10 through a line L10.
The first reactor 10 is a reactor for obtaining methacrolein from isobutylene and/or TBA and oxygen. The first reactor 10 is preferably a reactor in which a vessel is filled with a catalyst. The first reactor 10 may be a fixed bed reactor in which a catalyst is filled in a vessel. The direction of the flow is not limited and may be upward or downward. Examples of the catalyst used in the reaction for synthesizing methacrolein from isobutylene and/or TBA and oxygen are metal oxides containing molybdenum and bismuth.
In the case of obtaining methacrolein from isobutylene and oxygen, isobutylene reacts with oxygen, thereby producing methacrolein. TBA may also be used in place of isobutylene. When methacrolein is obtained from TBA and oxygen, it is considered that isobutylene is produced by dehydration reaction of TBA, and the produced isobutylene reacts with oxygen to produce methacrolein. The reason why TBA can be used instead of isobutylene is considered to be that the oxidation reaction of isobutylene in the first reactor 10 is a rate-limiting step. Isobutylene and TBA may also be used in combination.
The outlet 10j of the first reactor 10 and the inlet 20i of the second reactor 20 are connected by a line LA.
Inlet 50b of gas mixer 50b of line LB and line LAmAnd (4) connecting. Line LB is a line connecting line LA and the oxygen supply source (S1).
The second reactor 20 is a reactor for obtaining methacrylic acid by reacting methacrolein and oxygen. The second reactor 20 is preferably a reactor in which a container is filled with a catalyst. The second reactor 20 may be a fixed bed reactor in which a catalyst is filled in a vessel. The direction of the flow is not limited and may be upward or downward. Examples of the catalyst used in the reaction for synthesizing methacrylic acid from methacrolein and oxygen are heteropoly acid compounds containing phosphorus and molybdenum.
The outlet 20j of the second reactor 20 is connected to the liquid inlet 70i of the methacrolein recovery unit 70 via the liquefaction unit 60 and through the line LC. Liquefaction unit 60 has one inlet and three outlets. Line LC is connected to the inlet and one outlet of liquefaction unit 60, and line L35 and line L31 are connected to the other two outlets, respectively.
The liquefaction unit 60 is a unit that liquefies methacrylic acid and unreacted methacrolein in the stream (F30) of the outlet gas of the second reactor 20. The liquefaction unit 60 may have a function of separating methacrolein. Examples of the liquefaction unit 60 include: distillation columns, extraction columns, absorption columns, and combinations thereof. The number of inlets and outlets of the liquefaction unit 60 may vary depending on the form of the liquefaction unit 60. For example, there may be line L35 and line L31, or there may be no line L35 and line L31. Further, other lines not shown may be connected to the liquefaction unit 60.
The methacrolein recovery unit 70 is a unit that recovers methacrolein. The methacrolein recovery unit 70 includes: a liquid inlet 70i, a liquid outlet 70j, and a gas outlet 70 gj. Examples of the methacrolein recovery unit 70 include: a stripper column, a distillation column, and combinations thereof. In the stripping column, a liquid containing methacrolein is brought into contact with a stripping gas, and methacrolein is separated by accompanying the stripping gas with the methacrolein.
In the case where the methacrolein recovery unit 70 is a stripper, as shown in fig. 1, the methacrolein recovery unit 70 has a gas inlet 70gi in addition to a liquid inlet 70i, a liquid outlet 70j and a gas outlet 70 gj. In the case where the methacrolein recovery unit 70 is a distillation column, the gas inlet 70gi is not necessarily required.
The gas outlet 70gj is preferably provided at the top of the methacrolein recovery unit 70 from the viewpoint of facilitating shortening of the length of the line from the gas outlet 70gj to the inlet 23i of the heating unit described later. The liquid outlet 70j is provided at the bottom of the methacrolein recovery unit 70, for example.
The line L40 is connected to the liquid outlet 70j of the methacrolein recovery unit 70. Line L40 merges with line L31.
The gas outlet 70gj of the methacrolein recovery unit 70 and the line LA are connected by a line LD.
The heating unit 23a is provided on a part of the line from the gas outlets 70gj to Xm. Here, assuming that the length of the line from the gas outlet 70gj to the connection Xo with the line LA is 100, the length of the line from the gas outlet 70gj to Xm is 30 or less. That is, when the length of the line from the gas outlet 70gj to the connection Xo with the line LA is 100, the heating unit 23a is disposed on at least a part of the line from the gas outlet 70gj to a position where the length of the line is 30. Here, the length of the pipeline refers to the length of the central axis of the pipeline. In addition, the heating unit 23a is a part of the pipeline.
From the viewpoint of further improving the continuous operability, when the length of the line from the gas outlet 70gj to the connection Xo with the line LA is set to 100, the heating unit 23a is preferably arranged on at least a part of the line from the gas outlet 70gj to a position where the length of the line is 20, and more preferably on at least a part of the line from the gas outlet 70gj to a position where the length of the line is 10.
As the heating unit 23a, there can be mentioned: heat exchangers, jacketed piping, tubing wrapped with sheet heaters, and the like.
From the viewpoint of further improving the continuous operability, the length of the line from the gas outlet 70gj to the inlet 23i of the heating unit 23a is preferably 3m or less. The heating unit 23a may be directly provided at the gas outlet 70 gj. From the viewpoints of continuous operability and simplification of the apparatus, the gas outlet 70gj may be provided at the top of the methacrolein recovery unit 70, and the heating unit 23a may be directly provided at the gas outlet 70 gj.
Next, a method for producing methacrylic acid according to the present embodiment will be described.
(supply source)
A stream (F10) containing isobutylene and/or TBA and oxygen is prepared as a supply source (S0) of a gas containing isobutylene and/or TBA and oxygen.
The stream (F10) may contain constituents other than isobutylene, TBA and oxygen. Examples of the components other than isobutylene, TBA and oxygen include: c5 olefins such as isoprene, isobutane, 1-butene, 2-butene (cis, trans), propane, propylene, n-butane, methyl tert-butyl ether, methanol, dimethyl ether, butadiene, propadiene, diisobutylene, nitrogen, carbon monoxide, carbon dioxide, water and argon.
The concentration of isobutene and/or TBA in the stream (F10) is, for example, 1 mass% or more, 2 mass% or more or 4 mass% or more, based on the sum of the concentrations of isobutene and TBA. The sum of the concentrations of isobutene and TBA in the stream (F10) is, for example, 21 mass% or less, 19 mass% or less, or 17 mass% or less. The sum of the concentrations of isobutylene and TBA in the stream (F10) is preferably 1 to 21 mass%, more preferably 2 to 19 mass%, and further preferably 4 to 17 mass%.
The oxygen concentration in the stream (F10) is, for example, 7 mass% or more, 8 mass% or more, or 10 mass% or more. The oxygen concentration in the stream (F10) is, for example, 24 mass% or less, 23 mass% or less, or 21 mass% or less. The oxygen concentration in the stream (F10) is preferably 7 to 24 mass%, more preferably 8 to 23 mass%, and still more preferably 10 to 21 mass%.
In addition, an oxygen-containing stream (F22) as an oxygen supply source (S1) was prepared.
The oxygen concentration in the stream (F22) is, for example, 15 mass% or more. The oxygen concentration in the stream (F22) is preferably 16% by mass or more, more preferably 17% by mass or more, and further preferably 20% by mass or more. The upper limit of the oxygen concentration in the stream (F22) may be set, for example, to 35 mass%. The oxygen concentration in the stream (F22) may be, for example, 30 mass% or less, or may be 25 mass% or less. The oxygen concentration in the stream (F22) is preferably 16 to 35 mass%, more preferably 17 to 30 mass%, and still more preferably 18 to 25 mass%.
(reaction procedure)
Stream (F10) is fed to first reactor 10, where isobutylene and oxygen in stream (F10) are reacted in first reactor 10. A stream (F11) containing methacrolein obtained by the reaction of isobutylene and oxygen was discharged from the line LA.
The reaction temperature of the first reactor 10 may be set to 300 to 400 ℃. The reaction pressure of the first reactor 10 may be set to 0.004MPaG to 0.6MPaG (gauge pressure).
A later-described recycle stream (F23) containing methacrolein and stripping gas is mixed in the stream (F11) discharged from the first reactor 10 via line LD and a stream (F22) containing oxygen is mixed via line LB. The stream thus obtained (F21) is fed to the second reactor 20 via line LA.
In the second reactor 20, methacrolein and oxygen are reacted to obtain methacrylic acid, and a stream containing methacrylic acid is discharged through the line LC (F30).
Stream (F30) contains unreacted methacrolein. Stream (F30) may contain components other than methacrylic acid and methacrolein. Examples of such components include: acrylic acid, acrolein, nitrogen, argon, water, carbon monoxide, carbon dioxide, acetaldehyde, propionaldehyde, terephthalic acid, maleic acid, fumaric acid, diacetyl, isophthalic acid, isobutyric acid, methylfurfural, acetic acid, propionic acid, and the like.
The reaction temperature of the second reactor 20 may be set to 200 to 350 ℃. The reaction pressure in the second reactor 20 is, for example, 0.01MPaG to 0.3 MPaG.
(liquefaction Process)
The stream (F30) coming out of the second reactor 20 is supplied to the liquefaction unit 60 through the line LC. In the liquefaction unit 60, methacrylic acid and methacrolein in the stream (F30) are liquefied, for example, a stream containing methacrylic acid and heavy components (F31) is withdrawn from line L31, a stream containing carbon monoxide, carbon dioxide, nitrogen, argon, other light components and oxygen (F35) is withdrawn from line L35, and a stream containing methacrolein (F34) is withdrawn from line LC.
(Methylacrolein recovery step)
The methacrolein-containing stream (F34) is supplied to the methacrolein recovery unit 70 through the line LC.
In the case where the methacrolein recovery unit 70 is a stripping column, a stream containing a stripping gas is supplied to the gas inlet 70gi, a stream containing methacrylic acid and heavy components is discharged from the liquid outlet 70j (F40), and a stream containing methacrolein and a stripping gas is discharged from the gas outlet 70gj (F23). The stripping gas may be any gas which can strip out methacrolein when it comes into contact with a liquid containing methacrolein. The stripping gas may contain at least one gaseous component selected from the group consisting of nitrogen, argon, oxygen, and carbon dioxide.
In the case where the methacrolein recovery unit 70 is a distillation column, it suffices to discharge, for example, a stream containing methacrylic acid and heavy components (F40) from the liquid outlet 70j and a stream containing methacrolein (F23) from the gas outlet 70gj by a distillation operation.
The temperature of the stream (F23) at the gas outlet 70gj of the methacrolein recovery unit 70 may be, for example, 50 to 90 ℃, or 55 to 85 ℃, or 60 to 80 ℃.
The concentration of methacrolein in the stream (F23) is preferably 0.1% by mass or more, more preferably 3% by mass or more, further preferably 7% by mass or more. The concentration of methacrolein in the stream (F23) is preferably 32% by mass or less, more preferably 23% by mass or less, further preferably 16% by mass or less. The concentration of methacrolein in the stream (F23) may be from 0.1% by mass to 32% by mass, may also be from 3% by mass to 23% by mass, and may also be from 7% by mass to 16% by mass. Stream (F23) may contain, for example, nitrogen, argon, oxygen, water and carbon dioxide as components other than methacrolein.
Stream (F40) is combined with stream (F31).
Stream (F23) is heated using heating unit 23 a. The temperature of the heated stream (F23) may be, for example, 150 ℃ or higher, 170 ℃ or higher, or 190 ℃ or higher. The temperature of the heated stream (F23) may be, for example, 285 ℃ or less, 250 ℃ or less, or 220 ℃ or less. The temperature of the heated stream (F23) can be, for example, from 150 ℃ to 285 ℃, also from 170 ℃ to 250 ℃, and also from 190 ℃ to 220 ℃.
The stream (F23) heated by the heating unit 23a is joined as a recycle stream with the stream (F11).
The apparatus 100 for producing methacrylic acid includes: a first reactor 10, said first reactor 10 having an inlet 10i and an outlet 10j and being for obtaining methacrolein from isobutylene and/or TBA and oxygen; a second reactor 20 having an inlet 20i and an outlet 20j and for obtaining methacrylic acid by reacting methacrolein and oxygen; a methacrolein recovery unit 70, the methacrolein recovery unit 70 having a liquid inlet 70i, a liquid outlet 70j, and a gas outlet 70 gj; a line LA connecting the outlet 10j of the first reactor 10 and the inlet 20i of the second reactor 20; a line LB connecting the line LA and the oxygen supply source (S1); a line LC connecting the outlet 20j of the second reactor 20 and the liquid inlet 70i of the methacrolein recovery unit 70; and a line LD connecting the gas outlet 70gj of the methacrolein recovery unit 70 and the line LA, the line LD having a heating unit disposed on at least a part of the line from the gas outlet 70gj to a position where the length of the line is 30, when the length of the line from the gas outlet 70gj to the connection part Xo is set to 100. This provides excellent continuous operability. The reason why the inventors surmised that the continuous operability was excellent in such a device is as follows.
Consider that: in the case where methacrolein recovered from the gas outlet of the methacrolein recovery unit 70 is recycled to the second reactor, methacrolein liquefies and polymerizes, or heavy components are precipitated, while recycling at the temperature as it is. Further, when the continuous operation is continued as it is, there is a possibility that the amount of methacrolein recycled from the methacrolein recovery unit 70 to the second reactor is reduced, and as a result, the productivity of methacrylic acid is lowered. In addition, it is considered that: the amount of the recycled methacrolein affects the composition of the components at the inlet of the second reactor, and thus affects the reaction in the second reactor. Along with this, continuous operation may become difficult. In contrast, it is considered that: in the apparatus for producing methacrylic acid 100, since the heating means 23a is provided at the above-mentioned position of the line LD, liquefaction of methacrolein and deposition of heavy components are easily reduced, and the second reactor is easily maintained in a stable state. Therefore, even in the case of long-term operation, stable operation is facilitated, and continuous operability is excellent.
Further, since the apparatus of the present embodiment is excellent in continuous operability, it is considered that the raw material and energy during long-term operation can be reduced.
The present invention is not limited to the above embodiment, and various modifications are possible.
For example, each of the first reactor 10 and the second reactor 20 may be a reactor in which a plurality of unit reactors are connected in series or in parallel, and a separation and purification unit such as a distillation column or an extraction column may be further added to each line.
Line L40 may not necessarily merge with line L31. That is, the stream (F40) and the stream (F31) may each be sent to the next process separately.
The gas mixer 50b may be omitted. In this case, line LB may be connected directly to the pipe of line LA.
In the apparatus for producing methacrylic acid 100, the heating means 23a is disposed in a part of the line from the gas outlet 70gj to the position where the line length is 30, assuming that the line length from the gas outlet 70gj to the connection Xo with the line LA is 100, but the heating means may be disposed in all lines from the gas outlet 70gj to the position where the line length is 30.
The line LD may have other heating units in locations other than the location from the gas outlet 70gj to the location where the length of the line is 30.

Claims (4)

1. An apparatus for producing methacrylic acid, comprising:
a first reactor having an inlet and an outlet and for obtaining methacrolein from isobutylene and/or tert-butanol and oxygen;
a second reactor having an inlet and an outlet and for obtaining methacrylic acid by reacting methacrolein and oxygen;
a methacrolein recovery unit having a liquid inlet, a liquid outlet, and a gas outlet;
a line LA connecting the outlet of the first reactor and the inlet of the second reactor;
a line LB connecting the line LA and an oxygen supply source;
a line LC connecting an outlet of the second reactor and a liquid inlet of the methacrolein recovery unit; and
a line LD connecting a gas outlet of the methacrolein recovery unit and the line LA,
the line LD is provided with a heating unit,
the heating unit is disposed on at least a part of the pipeline between the gas outlet and a position where the length of the pipeline is 30, when the length of the pipeline from the gas outlet to the connection Xo with the pipeline LA is set to 100.
2. The apparatus for producing methacrylic acid according to claim 1, wherein the heating unit is disposed on at least a part of the line from the gas outlet to a position where the line has a length of 20.
3. The apparatus for producing methacrylic acid according to claim 1 or 2, wherein the heating unit is disposed on at least a part of the line from the gas outlet to a position where the line has a length of 10.
4. The apparatus for producing methacrylic acid according to any one of claims 1 to 3, wherein a length of a line from the gas outlet to an inlet of the heating unit is 3m or less.
CN201911069670.8A 2018-11-14 2019-11-05 Apparatus for producing methacrylic acid Pending CN110903184A (en)

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Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB2096601A (en) * 1981-03-04 1982-10-20 Japan Synthetic Rubber Co Ltd Process for producing methacrylic acid
JP2003103105A (en) * 2001-09-28 2003-04-08 Sumitomo Chem Co Ltd Distillation method for easily polymerizable substance and distillation apparatus used for the same
CN1642893A (en) * 2002-03-28 2005-07-20 三菱丽阳株式会社 Transporting method and transporting facility for easily polymerizable material
CN106457062A (en) * 2014-06-12 2017-02-22 巴斯夫欧洲公司 Crystallisation apparatus and process
CN106631759A (en) * 2016-12-09 2017-05-10 中国化学赛鼎宁波工程有限公司 System and method for simultaneously producing methacrylic acid and methacrolein

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP1994978A1 (en) 2007-05-25 2008-11-26 Evonik Röhm GmbH Process for preparation of methyl methacrylate by esterification during oxidation

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB2096601A (en) * 1981-03-04 1982-10-20 Japan Synthetic Rubber Co Ltd Process for producing methacrylic acid
JP2003103105A (en) * 2001-09-28 2003-04-08 Sumitomo Chem Co Ltd Distillation method for easily polymerizable substance and distillation apparatus used for the same
CN1642893A (en) * 2002-03-28 2005-07-20 三菱丽阳株式会社 Transporting method and transporting facility for easily polymerizable material
CN106457062A (en) * 2014-06-12 2017-02-22 巴斯夫欧洲公司 Crystallisation apparatus and process
CN106631759A (en) * 2016-12-09 2017-05-10 中国化学赛鼎宁波工程有限公司 System and method for simultaneously producing methacrylic acid and methacrolein

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
李景田等: "《管道与设备保温》", 31 August 1984 *

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JP6611391B1 (en) 2019-11-27

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