WO2015030470A1 - (메트)아크릴산의 연속 회수 방법 및 장치 - Google Patents
(메트)아크릴산의 연속 회수 방법 및 장치 Download PDFInfo
- Publication number
- WO2015030470A1 WO2015030470A1 PCT/KR2014/007944 KR2014007944W WO2015030470A1 WO 2015030470 A1 WO2015030470 A1 WO 2015030470A1 KR 2014007944 W KR2014007944 W KR 2014007944W WO 2015030470 A1 WO2015030470 A1 WO 2015030470A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- acrylic acid
- meth
- extraction
- distillation
- column
- Prior art date
Links
- CERQOIWHTDAKMF-UHFFFAOYSA-N Methacrylic acid Chemical compound CC(=C)C(O)=O CERQOIWHTDAKMF-UHFFFAOYSA-N 0.000 title claims abstract description 227
- 238000000034 method Methods 0.000 title claims abstract description 79
- 238000004821 distillation Methods 0.000 claims description 170
- 238000000605 extraction Methods 0.000 claims description 112
- 238000010521 absorption reaction Methods 0.000 claims description 80
- 239000002904 solvent Substances 0.000 claims description 72
- 239000007864 aqueous solution Substances 0.000 claims description 68
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 42
- 239000000284 extract Substances 0.000 claims description 40
- 239000007788 liquid Substances 0.000 claims description 29
- 238000011084 recovery Methods 0.000 claims description 28
- 239000006227 byproduct Substances 0.000 claims description 27
- 239000000243 solution Substances 0.000 claims description 25
- 238000012546 transfer Methods 0.000 claims description 24
- 238000006243 chemical reaction Methods 0.000 claims description 4
- 238000007599 discharging Methods 0.000 claims 1
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 78
- 239000007789 gas Substances 0.000 description 40
- SMZOUWXMTYCWNB-UHFFFAOYSA-N 2-(2-methoxy-5-methylphenyl)ethanamine Chemical compound COC1=CC=C(C)C=C1CCN SMZOUWXMTYCWNB-UHFFFAOYSA-N 0.000 description 36
- NIXOWILDQLNWCW-UHFFFAOYSA-N 2-Propenoic acid Natural products OC(=O)C=C NIXOWILDQLNWCW-UHFFFAOYSA-N 0.000 description 36
- 238000009835 boiling Methods 0.000 description 16
- 238000005191 phase separation Methods 0.000 description 15
- 239000012071 phase Substances 0.000 description 13
- 230000000052 comparative effect Effects 0.000 description 12
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 10
- IMNFDUFMRHMDMM-UHFFFAOYSA-N N-Heptane Chemical compound CCCCCCC IMNFDUFMRHMDMM-UHFFFAOYSA-N 0.000 description 9
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 9
- 239000000203 mixture Substances 0.000 description 9
- 238000007254 oxidation reaction Methods 0.000 description 8
- 238000003786 synthesis reaction Methods 0.000 description 8
- 150000001875 compounds Chemical class 0.000 description 7
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 6
- 239000008346 aqueous phase Substances 0.000 description 6
- 239000003054 catalyst Substances 0.000 description 6
- 230000002209 hydrophobic effect Effects 0.000 description 6
- 239000012044 organic layer Substances 0.000 description 6
- 238000010992 reflux Methods 0.000 description 6
- 239000012074 organic phase Substances 0.000 description 5
- 238000006116 polymerization reaction Methods 0.000 description 5
- 239000001294 propane Substances 0.000 description 5
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 5
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 5
- ZGEGCLOFRBLKSE-UHFFFAOYSA-N 1-Heptene Chemical compound CCCCCC=C ZGEGCLOFRBLKSE-UHFFFAOYSA-N 0.000 description 4
- WGECXQBGLLYSFP-UHFFFAOYSA-N 2,3-dimethylpentane Chemical compound CCC(C)C(C)C WGECXQBGLLYSFP-UHFFFAOYSA-N 0.000 description 4
- YNQLUTRBYVCPMQ-UHFFFAOYSA-N Ethylbenzene Chemical compound CCC1=CC=CC=C1 YNQLUTRBYVCPMQ-UHFFFAOYSA-N 0.000 description 4
- IFTRQJLVEBNKJK-UHFFFAOYSA-N Ethylcyclopentane Chemical compound CCC1CCCC1 IFTRQJLVEBNKJK-UHFFFAOYSA-N 0.000 description 4
- 238000010533 azeotropic distillation Methods 0.000 description 4
- DKPFZGUDAPQIHT-UHFFFAOYSA-N butyl acetate Chemical compound CCCCOC(C)=O DKPFZGUDAPQIHT-UHFFFAOYSA-N 0.000 description 4
- DMEGYFMYUHOHGS-UHFFFAOYSA-N cycloheptane Chemical compound C1CCCCCC1 DMEGYFMYUHOHGS-UHFFFAOYSA-N 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- UAEPNZWRGJTJPN-UHFFFAOYSA-N methylcyclohexane Chemical compound CC1CCCCC1 UAEPNZWRGJTJPN-UHFFFAOYSA-N 0.000 description 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N monobenzene Natural products C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 4
- YKYONYBAUNKHLG-UHFFFAOYSA-N propyl acetate Chemical compound CCCOC(C)=O YKYONYBAUNKHLG-UHFFFAOYSA-N 0.000 description 4
- 238000000926 separation method Methods 0.000 description 4
- RCBGGJURENJHKV-UHFFFAOYSA-N 2-methylhept-1-ene Chemical compound CCCCCC(C)=C RCBGGJURENJHKV-UHFFFAOYSA-N 0.000 description 3
- 239000001569 carbon dioxide Substances 0.000 description 3
- 229910002092 carbon dioxide Inorganic materials 0.000 description 3
- 238000009833 condensation Methods 0.000 description 3
- 230000005494 condensation Effects 0.000 description 3
- ZXIJMRYMVAMXQP-UHFFFAOYSA-N cycloheptene Chemical compound C1CCC=CCC1 ZXIJMRYMVAMXQP-UHFFFAOYSA-N 0.000 description 3
- 238000001704 evaporation Methods 0.000 description 3
- 230000008020 evaporation Effects 0.000 description 3
- 239000011261 inert gas Substances 0.000 description 3
- 239000010410 layer Substances 0.000 description 3
- GPDFVOVLOXMSBT-UHFFFAOYSA-N 1-propan-2-yloxybutane Chemical compound CCCCOC(C)C GPDFVOVLOXMSBT-UHFFFAOYSA-N 0.000 description 2
- BZHMBWZPUJHVEE-UHFFFAOYSA-N 2,3-dimethylpentane Natural products CC(C)CC(C)C BZHMBWZPUJHVEE-UHFFFAOYSA-N 0.000 description 2
- IRUDSQHLKGNCGF-UHFFFAOYSA-N 2-methylhex-1-ene Chemical compound CCCCC(C)=C IRUDSQHLKGNCGF-UHFFFAOYSA-N 0.000 description 2
- XTVRLCUJHGUXCP-UHFFFAOYSA-N 3-methyleneheptane Chemical compound CCCCC(=C)CC XTVRLCUJHGUXCP-UHFFFAOYSA-N 0.000 description 2
- JIUFYGIESXPUPL-UHFFFAOYSA-N 5-methylhex-1-ene Chemical compound CC(C)CCC=C JIUFYGIESXPUPL-UHFFFAOYSA-N 0.000 description 2
- DGINPNITKMCAJQ-UHFFFAOYSA-N 6-methylhept-1-ene Chemical compound CC(CCCC=C)C.CC(CCCC=C)C DGINPNITKMCAJQ-UHFFFAOYSA-N 0.000 description 2
- HGINCPLSRVDWNT-UHFFFAOYSA-N Acrolein Chemical compound C=CC=O HGINCPLSRVDWNT-UHFFFAOYSA-N 0.000 description 2
- NIXOWILDQLNWCW-UHFFFAOYSA-M Acrylate Chemical compound [O-]C(=O)C=C NIXOWILDQLNWCW-UHFFFAOYSA-M 0.000 description 2
- RTZKZFJDLAIYFH-UHFFFAOYSA-N Diethyl ether Chemical compound CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 description 2
- VQTUBCCKSQIDNK-UHFFFAOYSA-N Isobutene Chemical group CC(C)=C VQTUBCCKSQIDNK-UHFFFAOYSA-N 0.000 description 2
- NTIZESTWPVYFNL-UHFFFAOYSA-N Methyl isobutyl ketone Chemical compound CC(C)CC(C)=O NTIZESTWPVYFNL-UHFFFAOYSA-N 0.000 description 2
- UIHCLUNTQKBZGK-UHFFFAOYSA-N Methyl isobutyl ketone Natural products CCC(C)C(C)=O UIHCLUNTQKBZGK-UHFFFAOYSA-N 0.000 description 2
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical compound CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 description 2
- 239000001273 butane Substances 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 238000002425 crystallisation Methods 0.000 description 2
- 230000008025 crystallization Effects 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- 230000009977 dual effect Effects 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 229940058172 ethylbenzene Drugs 0.000 description 2
- 239000000706 filtrate Substances 0.000 description 2
- 238000001914 filtration Methods 0.000 description 2
- 239000003112 inhibitor Substances 0.000 description 2
- GJRQTCIYDGXPES-UHFFFAOYSA-N iso-butyl acetate Natural products CC(C)COC(C)=O GJRQTCIYDGXPES-UHFFFAOYSA-N 0.000 description 2
- FGKJLKRYENPLQH-UHFFFAOYSA-M isocaproate Chemical compound CC(C)CCC([O-])=O FGKJLKRYENPLQH-UHFFFAOYSA-M 0.000 description 2
- JMMWKPVZQRWMSS-UHFFFAOYSA-N isopropanol acetate Natural products CC(C)OC(C)=O JMMWKPVZQRWMSS-UHFFFAOYSA-N 0.000 description 2
- 229940011051 isopropyl acetate Drugs 0.000 description 2
- GWYFCOCPABKNJV-UHFFFAOYSA-N isovaleric acid Chemical compound CC(C)CC(O)=O GWYFCOCPABKNJV-UHFFFAOYSA-N 0.000 description 2
- OQAGVSWESNCJJT-UHFFFAOYSA-N isovaleric acid methyl ester Natural products COC(=O)CC(C)C OQAGVSWESNCJJT-UHFFFAOYSA-N 0.000 description 2
- 229940043265 methyl isobutyl ketone Drugs 0.000 description 2
- GYNNXHKOJHMOHS-UHFFFAOYSA-N methyl-cycloheptane Natural products CC1CCCCCC1 GYNNXHKOJHMOHS-UHFFFAOYSA-N 0.000 description 2
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 2
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 2
- 230000003647 oxidation Effects 0.000 description 2
- 238000012856 packing Methods 0.000 description 2
- 125000001997 phenyl group Chemical group [H]C1=C([H])C([H])=C(*)C([H])=C1[H] 0.000 description 2
- 229920000642 polymer Polymers 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 239000007921 spray Substances 0.000 description 2
- 239000008096 xylene Substances 0.000 description 2
- CFVWNXQPGQOHRJ-UHFFFAOYSA-N 2-methylpropyl prop-2-enoate Chemical compound CC(C)COC(=O)C=C CFVWNXQPGQOHRJ-UHFFFAOYSA-N 0.000 description 1
- WHRSAPITCBEUMU-UHFFFAOYSA-N 2-methylpropyl prop-2-enoate;prop-2-enoic acid Chemical compound OC(=O)C=C.CC(C)COC(=O)C=C WHRSAPITCBEUMU-UHFFFAOYSA-N 0.000 description 1
- BFGOGLKYJXQPJZ-UHFFFAOYSA-N 4-methylhept-1-ene Chemical compound CCCC(C)CC=C BFGOGLKYJXQPJZ-UHFFFAOYSA-N 0.000 description 1
- RJIGCBNUGDSREW-UHFFFAOYSA-N CC(CC=C)CCC.CC(CC=C)CCC Chemical compound CC(CC=C)CCC.CC(CC=C)CCC RJIGCBNUGDSREW-UHFFFAOYSA-N 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- RRHGJUQNOFWUDK-UHFFFAOYSA-N Isoprene Chemical compound CC(=C)C=C RRHGJUQNOFWUDK-UHFFFAOYSA-N 0.000 description 1
- BQCADISMDOOEFD-UHFFFAOYSA-N Silver Chemical compound [Ag] BQCADISMDOOEFD-UHFFFAOYSA-N 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 230000002745 absorbent Effects 0.000 description 1
- 239000006286 aqueous extract Substances 0.000 description 1
- 239000003125 aqueous solvent Substances 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 238000010924 continuous production Methods 0.000 description 1
- 239000006184 cosolvent Substances 0.000 description 1
- 239000000539 dimer Substances 0.000 description 1
- 238000007429 general method Methods 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- IGOCVOLAIVMTKD-UHFFFAOYSA-N hept-1-ene Chemical compound C=CCCCCC.C=CCCCCC IGOCVOLAIVMTKD-UHFFFAOYSA-N 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 230000000704 physical effect Effects 0.000 description 1
- 238000011112 process operation Methods 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 229910052709 silver Inorganic materials 0.000 description 1
- 239000004332 silver Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 230000002194 synthesizing effect Effects 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07B—GENERAL METHODS OF ORGANIC CHEMISTRY; APPARATUS THEREFOR
- C07B63/00—Purification; Separation; Stabilisation; Use of additives
-
- 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
Definitions
- the present invention relates to a method and apparatus for continuous recovery of (meth) acrylic acid.
- (Meth) acrylic acid is generally produced by a method of reacting gas phase oxidation in the presence of a catalyst with a compound such as propane, propylene, (meth) acrelane and the like.
- propane, propylene, etc. are converted to (meth) acrylic acid via (meth) arlane by gas phase oxidation reaction, and (meth) acrylic acid, unreacted propane or
- a reaction product mixed gas comprising propylene, (meth) arklane, an inert gas, carbon dioxide, water vapor and various organic by-products (such as acetic acid, low boiling point by-products, high boiling point by-products, etc.) is obtained.
- the (meth) acrylic acid-containing gas is heunhap (meth) in contact with the absorption _ solvent containing water in the acrylic acid absorption column is recovered as (meth) acrylic acid aqueous solution. Then, the insoluble gas from which (meth) acrylic acid is degassed is recycled to the synthesis reaction of (meth) acrylic acid, and part of it is incinerated to be converted into a harmless gas and discharged.
- the (meth) acrylic acid aqueous solution is obtained as (meth) acrylic acid through a process such as extraction, distillation and purification.
- a method of azeotropic distillation using a hydrophobic solvent in a distillation column 300 is known as a method for separating water and acetic acid from an aqueous (meth) acrylic acid solution obtained in a (meth) acrylic acid absorption tower.
- a method of supplying an aqueous (meth) acrylic acid solution to an extraction column to obtain a (meth) acrylic acid extract with reduced water content and a balance thereof and distilling the extract to obtain (meth) acrylic acid is known.
- the present invention provides a method for continuously recovering (meth) acrylic acid, which can minimize the loss of (meth) acrylic acid in a distillation process while enabling stable distillation operation and energy saving.
- this invention is providing the apparatus which can be used for the continuous collection
- a part of the (meth) acrylic acid aqueous solution obtained through the absorption process is contacted with an extraction solvent in an extraction column to obtain a (meth) acrylic acid extract through an upper outlet of the extraction column, and a lower outlet through a lower stationary section of the extraction column. Extraction process to obtain a balance through the; And
- the distillation process has a plurality of stages partitioned by perforated trays, and the perforated tubes located in the rectifying section relative to the feed point to which the feed is fed are stripped sections.
- a process for the continuous recovery of (meth) acrylic acid is provided, which is carried out in a distillation column having a lower opening ratio than the porous plates located in the stripping section.
- the distillation process may be performed in a distillation column having a ratio of the opening ratio of the porous plates positioned in the rectifying section based on the opening ratio of the porous plates positioned in the stripping section.
- the distillation process is characterized in that the porous plates are dual-flow It can be carried out in a distillation column which is a counter-current tray of dual-flow type.
- the feed point may be any point corresponding to 40 to 60% of the total stage from the top of the distillation column.
- (Meth) acrylic acid aqueous solution inlet to which a part of the (meth) acrylic acid aqueous solution is supplied through the aqueous solution outlet of the absorption tower 100 and the aqueous solution transfer line 102, and the contact of the introduced (meth) acrylic acid aqueous solution with the extraction solvent (Meth) acrylic acid extraction column provided with an extraction liquid outlet through which the (meth) acrylic acid extract obtained by is discharged, and a balance liquid outlet through which the residue obtained by contacting the (meth) acrylic acid aqueous solution and the extraction solvent is discharged (200) );
- the (meth) acrylic acid aqueous solution outlet of the absorption tower 100 and the aqueous solution transfer line (103) and the extraction liquid outlet of the extraction column 200 is connected through the extract liquid transfer line (203) to the (meth) acrylic acid aqueous solution Distillation column (300) having a feed point through which a feed containing the remainder of the extract and the extract is supplied, and a (meth) acrylic acid outlet through which (meth) acrylic acid obtained by distillation of the introduced feed is discharged Including,
- the distillation column has a plurality of stages partitioned by perforated trays, and the perforated plates in which the perforated plates located in the rectifying section relative to the feed point are located in the stripping section.
- a continuous recovery apparatus of (meth) acrylic acid is provided, having a lower opening ratio.
- the method and apparatus for continuous recovery of (meth) acrylic acid according to the present invention can minimize the loss of (meth) acrylic acid in the distillation process, while maintaining stable distillation. Enables operation of the process and energy savings.
- FIG. 1 schematically illustrates a general method and apparatus for continuous recovery of (meth) acrylic acid.
- FIG. 2 schematically illustrates a method and apparatus for continuous rare water of (meth) acrylic acid according to one embodiment of the present invention.
- FIG. 3 schematically illustrates a cross section of a distillation column applied to a method and apparatus for continuously recovering (meth) acrylic acid according to one embodiment of the present invention.
- Acrylic acid' may be used to mean acrylic acid, methacrylic acid, or a combination thereof.
- (meth) acrylic acid-containing mixed gas refers to a mixed gas that can be produced when synthesizing (meth) acrylic acid by gas phase oxidation reaction.
- Non-limiting examples include propane, propylene, butane, isobutylene, and
- the (meth) acrylic acid-containing mixed gas can be obtained by a gas phase oxidation reaction of at least one compound ('raw compound') selected from the group consisting of (meth) arklane in the presence of a catalyst.
- the (meth) acrylic acid-containing mixed gas may include (meth) acrylic acid, unreacted raw material compound, (meth) aclein, inert gas, carbon monoxide, carbon dioxide, water vapor, and various organic byproducts (acetic acid, low boiling point byproduct, high boiling point byproduct). Etc.) may be included.
- the poorly water-soluble suspended solids formed by the organic by-products are called scum.
- '(Meth) acrylic acid aqueous solution ⁇ is an aqueous solution containing (meth) acrylic acid, and can be obtained by, for example, contacting the (meth) acrylic acid-containing mixed gas with an absorption solvent containing water.
- the 'rectifying section' of a distillation column is the area above the feed point of the distillation column (e.g., the point at which the feed containing the aqueous (meth) acrylic acid solution and the (meth) acrylic acid extract is fed), In the distillation process, it means a region in which the concentration of a component having higher volatility among the components included in the feed increases.
- the term "stripping section" of the distillation column is a region below the feed point of the distillation column, and means a region in which the concentration of the more volatile components among the components included in the feed decreases during the distillation process. For example, in the distillation column 300 of FIG.
- the rectifying section 310 is the region from the feed point to the top of the distillation column, and the stripping section 390 is feed The area from the point to the bottom of the distillation column.
- a stage provided with the feed point in the distillation column is referred to as a 'feed stage'.
- perforated trays located in the rectifying section has a distillation column having a lower opening ratio than the porous plates located in the stripping section.
- the distillation process has a plurality of stages partitioned by perforated trays and the perforated plates located in the rectifying section relative to the feed point to which the feed is fed are stripped.
- a process for continuous recovery of (meth) acrylic acid is provided, which is carried out in a distillation column having a lower opening ratio than the porous plates located in the section.
- Continuous recovery method of (meth) acrylic acid according to an embodiment of the present invention, in particular, aims to minimize the loss of (meth) acrylic acid through the operation of a stable distillation process, to improve energy efficiency and productivity.
- the continuous recovery method of (meth) acrylic acid according to the present invention includes an absorption step of obtaining an aqueous (meth) acrylic acid solution, an extraction step for the aqueous (meth) acrylic acid solution, and the (meth) acrylic acid Distillation process for aqueous solution and extract.
- a distillation column having a structure as shown in FIG. 3 is used.
- the absorption step is a step for obtaining an aqueous (meth) acrylic acid solution.
- the (meth) acrylic acid-containing mixed gas obtained through the synthesis reaction of (meth) acrylic acid can be carried out by contacting with an absorption solvent including water.
- the synthesis reaction of (meth) acrylic acid may be performed by oxidizing reaction of at least one compound selected from the group consisting of propane, propylene, butane, isobutylene, and (meth) acrelane under a gas phase catalyst. Can be performed have. At this time, the gas phase oxidation reaction may be performed under the conditions of gas phase oxidation and reaction. Conventional catalysts in the gas phase oxidation reaction may also be used, and for example, the catalysts disclosed in Korean Patent Nos. 0349602 and 037818 may be used.
- the (meth) acrylic acid-containing mixed gas produced by the gas phase oxidation reaction includes, in addition to (meth) acrylic acid as a target product, unreacted raw compound, intermediate (meth) acrolein, inert gas, carbon dioxide, water vapor, and various organic by-products (acetic acid). , Low boiling by-products, high boiling by-products, etc.).
- the (meth) acrylic acid aqueous solution is obtained by supplying a (meth) acrylic acid-containing mixed gas (1) to the (meth) acrylic acid absorption tower 100 and contacting it with an absorption solvent containing water. Can lose.
- the type of the (meth) acrylic acid absorption tower 100 may be determined in consideration of the contact efficiency of the mixed gas 1 and the absorption solvent.
- the contact efficiency of the mixed gas 1 and the absorption solvent may be determined in consideration of the contact efficiency of the mixed gas 1 and the absorption solvent.
- the (meth) acrylic acid absorption tower 100 may be a packed tower or a multistage tray tower.
- the stratified tower may have a layering agent such as a rashing ring, a pall ring, a saddle, a gauze, and a structured packing.
- the mixed gas 1 may be supplied to the lower portion of the absorption tower 100, and the absorption solvent including water may be supplied to the upper portion of the absorption tower 100.
- the absorption solvent may include water such as scum water, demineralized water, and the like, and may include circulating water introduced from another process (eg, an aqueous phase recycled from an extraction process and / or a distillation process).
- the absorption solvent may contain a trace amount of organic by-products (for example, acetic acid) introduced from another process.
- (meth) is preferably in consideration of the absorption efficiency of acrylic acid absorption solvent (in particular the number of the rotation process) is fed to the absorption tower 100, such that the organic by-products are contained by more than 15 weight 0 /.
- the (raffinate solution) obtained in the (meth) acrylic acid extraction column (200) is recycled to the absorption tower 100 to be absorbed It can be used as a solvent.
- the (meth) acrylic acid absorption tower 100 has an internal pressure of 1 to 1.5 bar or 1 to 1.3 bar, in consideration of condensation conditions of the (meth) acrylic acid and moisture content conditions according to saturated steam pressure, and 50 to 100 ° C. Or it can be operated under an internal temperature of 50 to 80 ° C.
- the (meth) acrylic acid aqueous solution is discharged, and a noncondensable gas from which (meth) acrylic acid is degassed is discharged. At this time, to process efficiency such that the (meth) acrylic acid aqueous solution contains a concentration of 40% or more, or 40 to 90% by weight, or 50 to 90 weight 0/0, or 50 to 80 weight 0 /. Of (meth) acrylic acid It may be advantageous in terms of improvement.
- the obtained (meth) acrylic acid aqueous solution is supplied into the (meth) acrylic acid extraction column 200 and the distillation column 300 via aqueous solution transfer lines 102 and 103 as shown in FIG.
- the relaxation process rather than the method of sequentially passing through the extraction process and distillation process
- the distillation process can be operated under controlled operating conditions. In this way, the loss of (meth) acrylic acid in the distillation process can be further minimized, and the overall energy consumption can be reduced and stable process operation can be achieved.
- the ratio of dividing the aqueous (meth) acrylic acid solution to the extraction column 200 and the distillation column 300 may be determined by comprehensively considering the capacity, treatment performance, energy efficiency, and the like of each column. According to one embodiment, supplying the (meth) 5-70 increased 0 / acrylic acid aqueous solution., Or 10 to 60 parts by weight 0/0, or 10 to 50 parts by weight 0 /. To extraction column 200, the remainder May be advantageous in terms of the expression of the effects described above.
- the non-condensable gas discharged to the upper portion of the (meth) acrylic acid absorption tower 100 may be supplied to a process of recovering organic by-products (particularly acetic acid) included in the non-uniform gas, and the remaining waste gas incinerator. Can be disposed of and discarded. That is, according to one embodiment of the invention, the non-uniform gas In contact with the absorption solvent, a process of recovering acetic acid contained in the non-uniform gas may be performed. The process of contacting the non-uniform gas with the absorption solvent may be performed in the acetic acid absorption tower 150.
- an absorption solvent (process water) for absorbing acetic acid may be supplied to the upper portion of the acetic acid absorption tower 150, and an aqueous solution containing acetic acid may be discharged to the lower portion of the acetic acid absorption tower 150.
- the acetic acid-containing aqueous solution may be supplied to the upper portion of the (meth) acrylic acid absorption tower 100 and used as an absorption solvent.
- the non-condensable gas from which acetic acid is degassed may be circulated to the synthesis reaction process of (meth) acrylic acid and reused.
- the acetic acid absorption tower 150 may be operated under an internal pressure of 1 to 1.5 bar or 1 to 1.3 bar, and an internal temperature of 50 to 100 or 50 to 80 ° C.
- specific operating conditions of the acetic acid absorption tower 150 may be in accordance with the contents disclosed in the Republic of Korea Patent Publication No. 2009-0041355. Extraction process
- an extraction process is performed in which a part of the (meth) acrylic acid aqueous solution is contacted with an extraction solvent in an extraction column to obtain a (meth) acrylic acid extract and a balance thereof.
- the (meth) acrylic acid aqueous solution may be prepared through the above-described absorption process.
- the extraction process may be performed in the (meth) acrylic acid extraction column 200.
- the (meth) acrylic acid aqueous solution supplied to the extraction column 200 is in contact with the extraction solvent, and the extract solution in which a significant amount of (meth) acrylic acid is dissolved and a considerable amount of (meth) acrylic acid are lost.
- the relatively light phase of the extract is obtained through the upper outlet of the extraction column 200
- the relatively heavy phase of the extract is obtained through the bottom outlet of the extraction column.
- the balance liquid is present in a fixed amount in a fixed state in the lower stationary section of the extraction column, some of which is discharged to the lower outlet of the extraction column.
- the (meth) acrylic acid aqueous solution was extracted with the extraction solvent in the extraction column 200.
- a method of catalyzing ie, extracting less energy than distillation
- most of the water contained in the aqueous (meth) acrylic acid solution may be removed.
- the processing burden of the distillation process which is a subsequent process, can be reduced, and the energy efficiency of the entire process can be improved.
- polymerization reaction of (meth) acrylic acid that may occur during distillation can be minimized, and improved recovery efficiency of (meth) acrylic acid can be ensured.
- the balance may be supplied to the phase separation tank 350 through the balance transfer line 235 to be phase-separated into an aqueous phase and an organic phase together with the upper discharge of the distillation column 300.
- the balance may be circulated in the absorption process and used as an absorption solvent of (meth) acrylic acid.
- the extraction solvent supplied to the extraction column 200 may preferably have solubility and hydrophobicity for (meth) acrylic acid.
- the extraction solvent preferably has a lower boiling point than (meth) acrylic acid.
- the extraction solvent can be advantageous to operate the process in a hydrophobic solvent having a boiling point of 120 0 C or less, or from 10 to 120 ° C, or from 50 to 120 0 C.
- the extraction solvent is benzene, toluene, xylene, n-heptane, cycloheptane, cycloheptene, cycloheptene, 1-heptene (1 -heptene, ethyl-benzene, methyl-cyclohexane, n-butyl acetate, isobutyl acetate, isobutyl acrylate , n-propyl acetate, isopropyl acetate, methyl isobutyl ketone, 2-methyl-1-heptene, 2-methyl-1-heptene, 6-methyl -1 -heptene (6-methyl-1-heptene),
- the supply amount of the extraction solvent, the weight ratio of the extraction solvent to the aqueous solution of (meth) acrylic acid supplied to the extraction column 200 is 1: 1 to 1: 2, or 1: 1.0 to 1: 1.8, or 1: It can be adjusted in the range of 1.1 to 1: 1.5, or 1: 1 to 1: 1. That is, in order to ensure proper extraction efficiency, the extraction solvent is preferably maintained in a weight ratio of 1: 1 or more relative to the aqueous (meth) acrylic acid solution supplied to the extraction column 200.
- the extraction efficiency may be improved, but the loss of (meth) acrylic acid may be increased in the subsequent distillation column 300, and the azeotropic solvent may be Reflux flow can be excessively high, which is undesirable.
- the temperature of the (meth) acrylic acid aqueous solution supplied to the extraction column 200 is 10 to 70 0 C.
- the extraction column 200 in the extraction process a conventional extraction column according to the liquid-liquid contacting method may be used without particular limitation.
- the extraction column 200 may be a Karr type reciprocating plate column, a rotary-disk column, a contactor, a Scheibel column, a Kuhni column, a spray extraction column. extraction column, packed extraction column, pulsed packed column, and the like.
- the (meth) acrylic acid extract is discharged to the top of the extraction column 200, the discharged extract is supplied to the distillation column 300 through the transfer line (203). Then, the remaining balance is discharged to the lower portion of the extraction column 200, and the discharged balance can be recycled to the (meth) acrylic acid absorption tower 100 through the transfer line 201 after passing through a filtration system as necessary. have.
- the extract in addition to (meth) acrylic acid as the target compound, may include an extraction solvent, water, and an organic by-product.
- the extract in the normal state and a stable operation is performed, the extract has a (meth) acrylate, 30 to 40 parts by weight 0/0, the extraction solvent 55 to 65 parts by weight 0/0, water, 1 to 5 parts by weight 0/0, and Residual organic byproducts may be included. That is, through the extraction step (meth) acrylic acid contained in the aqueous solution of most of the water (e.g. 85 weight 0/0 over the water contained in the aqueous solution) which may be recovered as a weight balance.
- distillation conditions can be alleviated, such that polymerization reaction of (meth) acrylic acid can be minimized in the distillation process, such as securing operational stability and improving recovery efficiency of (meth) acrylic acid.
- the extraction liquid obtained through the lower outlet of the extraction column 200 may contain some (meth> acrylic acid) that is not extracted, except that, according to the above-described embodiment, the concentration may be 5 It increased 0 /. or less, or 0.5 to 5 wt%, or 1 to 3 can contain a (meth) acrylic acid having a weight 0/0, the (meth) loss of acrylic acid in the absorption step and the extraction step is minimized Can be.
- the feed may be a mixture of the remainder of the aqueous (meth) acrylic acid solution supplied from the above-described absorption process and the (meth) acrylic acid extract supplied from the aforementioned extraction process.
- the feed is supplied together to the feed point of the distillation column 300 through the (meth) acrylic acid aqueous solution transfer line 103 and the (meth) acrylic acid extract liquid transfer line 203 as shown in FIG. 2.
- the distillation process may be performed under distillation column 300 having a plurality of stages partitioned by perforated trays, as shown in FIG. 3.
- the stage means a place where condensation of steam moving to the top of the distillation column and evaporation of liquid moving to the bottom of the distillation column occur.
- the distillation process (meth) acrylic acid Based on the feed point at which the feed is included, the perforated plates located in the rectifying section 310 have a lower opening ratio than the perforated plates located in the stripping section 390. May be performed in column 300.
- the liquid level in the tekti Purifying section 310 and an upper region of the feed point (liquid level), flood 0/0 (Rood%), Prosper height (froth height), etc. was found to be much lower than in the stripping section 390, which is the lower region of the feed point.
- the amount of (meth) acrylic acid that is not recovered to the bottom of the distillation column but lost to the upper part in the distillation process increases, the consumption of azeotropic solvent used for distillation increases, and the temperature inside the distillation column is increased. It is confirmed that various problems occur, such as difficult to maintain a constant.
- the above-mentioned problems are solved in a distillation column in which the perforated trays located in the rectifying section 310 have a lower opening ratio than the perforated plates located in the stripping section 390.
- This can be solved by performing a distillation process. That is, based on the feed point of the distillation column 300, by varying the aperture ratio of the upper and lower porous plate, it is possible to reduce the difference of the hydraulic parameters (top and bottom). And, through this it is possible to minimize the loss of (meth) acrylic acid in the distillation process, it is possible to operate a stable distillation process and save energy.
- FIG. 2 by dividing and supplying the aqueous (meth) acrylic acid solution obtained through the absorption process into the extraction process and the distillation process, the distillation process can be performed under more relaxed operating conditions, which is advantageous for solving the problems. Do.
- the adjustment of the aperture ratio as described above can be more practical when the perforated plates are dual-flow type countercurrent trays without downcomer. have.
- the porous plates provided in the distillation column 300 may be of a cross-flow tray or a dual-flow type. Countercurrent trays.
- the cross-flow tray is provided with a weir and a downcomer, which may be relatively advantageous to maintain a liquid level of a certain height, but it is difficult to control the polymer generation caused by the distillation process. This may be unsuitable for commercial distillation processes. Accordingly, it is advantageous to apply a dual-flow type countercurrent tray in commercial distillation processes with high feed throughput.
- the dual-flow type is not equipped with a downcomer, it may be difficult to maintain a liquid level of a certain height.
- the opening ratio of the rectifying section 310 and the stripping section 390 is adjusted. As described above, the productivity can be improved.
- the distillation process based on the aperture ratio of the porous plates located in the stripping section 390, the ratio of the aperture ratios of the porous plates located in the rectifying section 310 (ie, located in the stripping section) Aperture ratio of the porous plates: aperture ratio of the porous tubes located in the rectifying section) 1: 0.6 to 1: 0.9, or 1: 0.65 to 1: 0.9, or 1: 0.65 to 1: 0.85, or 1: 0.65 to 1: 0.8 It is preferably carried out in distillation column 300.
- the aperture ratio of the porous plate located in the rectifying section 310 is compared to the aperture ratio of the porous plate positioned in the stripping section 390. It is advantageous to adjust it to 90% or less.
- the opening ratio of the rectifying section 310 is excessively low, the azeotropic solvent supplied to the top of the distillation column 300 may not be smoothly lowered to the feed point, even if the azeotropic solvent is lowered to the feed point The problem may arise in that the flood height of the rectifying section 310 is too high and flooding occurs.
- the opening ratio of the porous plate located in the rectifying section 310 is advantageously adjusted to 60% or more of the opening ratio of the porous plate located in the stripping section 390.
- the feed containing (meth) acrylic acid may be a mixture of the (meth) acrylic acid aqueous solution and (meth) acrylic acid extract.
- the feed is, through the (meth) acrylic acid aqueous solution transfer line 103 and (meth) acrylic acid extract liquid transfer line 203, as shown in FIG. May be fed to distillation column 300.
- the feed point is preferably increased Amboise of the distillation column (300). That is, the feed point may be any point corresponding to 40 to 60% of the entire stage from the top of the distillation column (300).
- the feed supplied to the distillation column 300 is brought into contact with the azeotropic solvent introduced into the upper portion of the distillation column 300, and is heated to an appropriate temperature to allow distillation by evaporation and condensation.
- the distillation is preferably performed by azeotropic distillation.
- the solvent applied to the azeotropic distillation method can be azeotropic with water and acetic acid, preferably a hydrophobic azeotropic solvent that does not azeotropic with (meth) acrylic acid.
- the hydrophobic azeotropic solvent preferably has a lower boiling point (for example, 120 ° C. or lower, or 10 to 120 ° C., or 50 to 120 boiling point) than (meth) acrylic acid.
- the hydrophobic azeotropic solvent is benzene, toluene, xylene, n-heptane, n-heptane, cycloheptane, cycloheptene, 1 ⁇ heptene ( 1 -heptene), ethyl-benzene, methyl-cyclohexane, n-butyl acetate, isobutyl acetate, isobutyl acrylate acrylate), n-propyl acetate, isopropyl acetate, methyl isobutyl ketone, 2-methyl-1 -heptene, 6 -Methyl-1 -heptene (6-methyl-1-heptene),
- the hydrophobic azeotropic solvent is extracted in the extraction process
- the same thing as a solvent is preferable.
- at least a part of the solvent distilled from the distillation column 300 and recovered through the phase separation tank 350 is supplied to the (meth) acrylic acid extraction column 200. It can be reused as an extraction solvent.
- the top discharge of the distillation column 300 may be supplied to the phase separation tank 350 may be reused after a predetermined treatment.
- the phase separation tank 350 is a device that separates the liquid phase that does not mix with each other by gravity or centrifugal force, etc.
- the relatively light liquid for example, the organic phase
- the relatively heavy liquid is a relatively heavy liquid to the top of the phase separation tank 350 (Eg, the water phase) may be recovered to the bottom of the phase separation tank 350.
- the upper effluent of the distillation column 300 may be separated into an organic phase including an azeotropic solvent and an aqueous phase including water in the phase separation tank 350.
- the extraction liquid in the aforementioned extraction process or the filtrate obtained by filtering the extraction liquid may be supplied to the phase separation tank 350 to be subjected to phase separation with the upper discharge liquid of the distillation column 300.
- the separated organic phase can be fed to the top of the distillation column 300 and used as an azeotropic solvent.
- at least a portion of the organic phase may be supplied to the extraction column 200 and used as an extraction solvent.
- at least a part of the aqueous phase separated from the phase separation tank 350 may be supplied to the (meth) acrylic acid absorption tower 100 to be used as an absorption solvent, and some may be treated with wastewater.
- the acetic acid may be partially contained in the aqueous phase, and the concentration of acetic acid included in the aqueous phase may vary depending on the type of azeotropic solvent and the reflux ratio.
- the concentration of acetic acid contained in the water phase may be 1 to 50 parts by weight 0/0, or 2 to 40 wt%, or 3 to 30 increased 0 /.
- the aqueous (meth) acrylic acid solution passes through the (meth) acrylic acid absorption tower 100, the extraction column 200, the distillation column 300, and the like, and at least a part of the (meth) acrylic acid included in the aqueous solution is a dimer. Or oligomers.
- distillation column (300) Conventional polymerization inhibitors may be added.
- the bottom discharge of the distillation column 300 may include high boiling point by-products such as polymers of (meth) acrylic acid, polymerization inhibitors, and the like, in addition to (meth) acrylic acid. Therefore, if necessary, a step of separating the high boiling by-products included in the lower discharge by supplying the bottom discharge of the distillation column 300 to the high boiling point by-product separation tower 400 may be performed. And, the crude (meth) acrylic acid (CAA) recovered through the above process may be obtained as a higher purity (meth) acrylic acid (HPAA) through an additional crystallization process. At this time, the high boiling point by-product separation process and crystallization process, etc. may be carried out under conventional conditions, the process conditions and the like are not limited.
- high boiling point by-product separation process and crystallization process, etc. may be carried out under conventional conditions, the process conditions and the like are not limited.
- each of the above-described steps can be performed organically and continuously.
- processes that may be normally performed before, after, or simultaneously with each step may be further included and operated.
- (Meth) acrylic acid aqueous solution inlet to which a part of the (meth) acrylic acid aqueous solution is supplied through the aqueous solution outlet of the absorption tower 100 and the aqueous solution transfer line 102, and the contact of the introduced (meth) acrylic acid aqueous solution and the extraction solvent (Meth) acrylic acid extraction column provided with an extraction liquid outlet through which the (meth) acrylic acid extract obtained by is discharged, and a balance liquid outlet through which the residue obtained by contacting the (meth) acrylic acid aqueous solution and the extraction solvent is discharged (200) );
- the (meth) acrylic acid aqueous solution outlet of the absorption tower 100 and the aqueous solution transfer line 103 are connected and the extract liquid outlet and the extract liquid of the extraction column 200 A feed point connected through a transfer line 203 to which a feed containing the rest of the aqueous (meth) acrylic acid solution and the extract is fed, and (meth) acrylic acid obtained by distillation of the feed introduced A distillation column 300 having a (meth) acrylic acid outlet being discharged,
- the distillation column has a plurality of stages partitioned by perforated trays, and the perforated tubes in which the perforated plates located in the rectifying section relative to the feed point are located in the stripping section.
- a continuous recovery apparatus of (meth) acrylic acid is provided, which has a lower opening ratio.
- FIG. 3 schematically illustrates a cross-sectional structure of a distillation column applied to a continuous recovery apparatus of (meth) acrylic acid according to one embodiment of the present invention.
- the distillation column 300 has a plurality of stages partitioned by perforated trays.
- the stage means a place where the expansion of the vapor moving to the top of the column and the evaporation of the liquid moving to the bottom of the column.
- the adjustment of the aperture ratio is better when the porous plates are dual-flow type countercurrent trays that are not provided with a downcomer. A substantial effect can be obtained.
- the ratio of the aperture ratios of the porous plates positioned in the rectifying section 310 based on the aperture ratios of the porous tubes positioned in the stripping section 390 of the distillation column 300 is 1: 0.6 to 1. Adjusted to: 0.9, or 1: 0.65 to 1: 0.9, or 1: 0.65 to 1: 0.85, or 1: 0.65 to 1: 0.8 It is preferable.
- the feed point is preferably the central portion of the distillation column (300). That is, the feed point may be any point corresponding to 40 to 60% of the entire stage from the top of the distillation column (300).
- the (meth) acrylic acid absorption tower 100 may be a packed tower or a multistage tray tower for improving the contact efficiency between the (meth) acrylic acid-containing mixed gas 1 and the absorption solvent.
- the stratified tower may have a layering agent such as a rashing ring, a pall ring, a saddle, a gauze, and a structured packing.
- the (meth) acrylic acid extraction column 200 a conventional extraction column according to a liquid-liquid contacting method may be applied without particular limitation.
- the extraction column 200 may be a Karr type reciprocating plate column, a rotary-disk contactor, a Scheibel column, a Kuhni column, a spray extraction column. column, packed extraction column, pulsed packed column, and the like.
- acetic acid absorption tower 150 (meth) acrylic acid aqueous solution transfer line 102, extract liquid transfer line 203, phase separation tank 350, high boiling point by-product separation tower 400, etc. It may be one having a conventional configuration in the field.
- preferred examples are provided to aid in understanding the present invention. However, the following examples are only for illustrating the present invention, and the present invention is not limited thereto.
- Aqueous acrylic acid solution (about 68 weight 0 /. Acrylic acid) was prepared through an acrylic acid absorption process, and the aqueous solution was distilled through a transfer line 103. Supplied to column 300.
- a dual flow tray pilot column (inner diameter 30 mm, total 28 stages, tray spacing 100 mm, porous plate opening ratio of about 23%) was prepared as the distillation column 300, and an operating pressure was maintained at about 1 10 torr.
- a feed comprising the aqueous acrylic acid solution was introduced at a flow rate of about 6.5 g / min from the top of the distillation column 300 to the location of the fourteenth stage.
- a reflux stream separated in the phase separation tank 350 as a cosolvent was introduced at a flow rate of about 1 1.95 g / min to the position of the first stage, which is the top of the distillation column 300.
- heat was supplied through a reboiler at the bottom of the distillation column (300).
- Heavies 0.00 0.00 0.00 0.00 0.20 As shown in Table 1, in Comparative Example 1, the concentration of acrylic acid in the upper organic layer flow of the distillation column was 0.08 weight 0 /., And the concentration of acrylic acid in the upper water layer flow was 0.76 weight. It was identified as a 0/0.
- Acrylic acid aqueous solution (acrylic acid about 68 weight 0 /.) Through acrylic acid absorption process and acrylic acid extract (about 32 weight 0 /. Acrylic acid, about 65 weight increase 0 /. The aqueous solution and the extract are then distilled at a weight ratio of about 4: 6 via respective transfer lines 103 and 203. Supplied to 3 ⁇ 4 lumber (300).
- a dual flow tray pilot column (inner diameter 30 mm, total 28 stages, tray spacing 100 mm, porous plate opening ratio of about 23%) was prepared as the distillation column 300, and the operating pressure was maintained at about "O torr.
- the prepared acrylic acid aqueous solution was supplied to the position of the 14th stage of the distillation column 300 at a flow rate of about 6.08 g / min, and the prepared acrylic acid extract was the 14th stage of the distillation column 300 at a flow rate of about 6.56 g / min. Was supplied at the position of.
- a reflux stream isolated from the phase separation bath 350 as an azeotropic solvent was introduced at a flow rate of about 7.68 g / min to the position of the first stage, which is the top of the distillation column 300.
- heat was supplied through a reboiler at the bottom of the distillation column (300).
- Acrylic acid flow was obtained.
- the top temperature of the distillation column 300 in the steady state was maintained at about 40 ° C, and the bottom temperature of the distillation column 300 was about 97 ° C, respectively.
- the upper part of the rectifying section is applied to the perforated plates having an opening of about 17%, and the lower part of the stripping section has an aperture ratio of about Acrylic acid flow was obtained in the same manner as in Comparative Example 3, except that 23% porous plates were applied. And the flow rate and composition in each process are shown in Table 4 below. .
- Example 3 In the case of Comparative Example 3, the temperature profile inside the distillation column was greatly shaken during operation. In contrast, in Example 1, the temperature profile inside the distillation column remained stable without shaking, and the ease of operation was also greatly improved.
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Crystallography & Structural Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
Description
Claims
Priority Applications (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US14/914,233 US10035751B2 (en) | 2013-08-30 | 2014-08-26 | Process for continuously recovering (meth)acrylic acid and apparatus for the process |
BR112016003892-4A BR112016003892B1 (pt) | 2013-08-30 | 2014-08-26 | processo para recuperação contínua do ácido met(acrílico) e dispositivo para o processo |
CN201480046775.0A CN105473541B (zh) | 2013-08-30 | 2014-08-26 | 用于连续回收(甲基)丙烯酸的方法和用于该方法的设备 |
US16/021,861 US10173956B1 (en) | 2013-08-30 | 2018-06-28 | Process for continuously recovering (meth)acrylic acid and apparatus for the process |
Applications Claiming Priority (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
KR10-2013-0104119 | 2013-08-30 | ||
KR20130104119 | 2013-08-30 | ||
KR10-2014-0110528 | 2014-08-25 | ||
KR1020140110528A KR101616553B1 (ko) | 2013-08-30 | 2014-08-25 | (메트)아크릴산의 연속 회수 방법 및 장치 |
Related Child Applications (2)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US14/914,233 A-371-Of-International US10035751B2 (en) | 2013-08-30 | 2014-08-26 | Process for continuously recovering (meth)acrylic acid and apparatus for the process |
US16/021,861 Division US10173956B1 (en) | 2013-08-30 | 2018-06-28 | Process for continuously recovering (meth)acrylic acid and apparatus for the process |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2015030470A1 true WO2015030470A1 (ko) | 2015-03-05 |
Family
ID=52586940
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/KR2014/007944 WO2015030470A1 (ko) | 2013-08-30 | 2014-08-26 | (메트)아크릴산의 연속 회수 방법 및 장치 |
Country Status (1)
Country | Link |
---|---|
WO (1) | WO2015030470A1 (ko) |
Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US20060000703A1 (en) * | 2002-12-03 | 2006-01-05 | Mason Robert M | High capacity purification of thermally unstable compounds |
US20090124825A1 (en) * | 2007-11-14 | 2009-05-14 | Shanghai Huayi Acrylic Acid Co., Ltd | Method of (meth) acrylate production |
JP2009242285A (ja) * | 2008-03-31 | 2009-10-22 | Mitsubishi Chemicals Corp | アクリル酸の製造方法 |
-
2014
- 2014-08-26 WO PCT/KR2014/007944 patent/WO2015030470A1/ko active Application Filing
Patent Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US20060000703A1 (en) * | 2002-12-03 | 2006-01-05 | Mason Robert M | High capacity purification of thermally unstable compounds |
US20090124825A1 (en) * | 2007-11-14 | 2009-05-14 | Shanghai Huayi Acrylic Acid Co., Ltd | Method of (meth) acrylate production |
JP2009242285A (ja) * | 2008-03-31 | 2009-10-22 | Mitsubishi Chemicals Corp | アクリル酸の製造方法 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
KR101546464B1 (ko) | (메트)아크릴산의 연속 회수 방법 및 회수 장치 | |
EP3404015B1 (en) | Method and apparatus for continuous recovery of (meth)acrylic acid | |
US11034642B2 (en) | Method and apparatus for continuously recovering (meth)acrylic acid | |
US9718756B2 (en) | Method for continuously recovering (meth)acrylic acid and apparatus for the method | |
US10173956B1 (en) | Process for continuously recovering (meth)acrylic acid and apparatus for the process | |
KR101659541B1 (ko) | (메트)아크릴산의 연속 회수 방법 | |
KR101601938B1 (ko) | (메트)아크릴산의 연속 회수 방법 및 회수 장치 | |
JP2019508477A (ja) | (メタ)アクリル酸の回収方法 | |
WO2016076559A1 (ko) | (메트)아크릴산의 연속 회수 방법 및 장치 | |
KR101628287B1 (ko) | (메트)아크릴산의 연속 회수 방법 및 장치 | |
KR101642504B1 (ko) | (메트)아크릴산의 연속 회수 방법 및 회수 장치 | |
WO2015030470A1 (ko) | (메트)아크릴산의 연속 회수 방법 및 장치 | |
KR20150011634A (ko) | (메트)아크릴산의 연속 회수 방법 및 회수 장치 |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
WWE | Wipo information: entry into national phase |
Ref document number: 201480046775.0 Country of ref document: CN |
|
121 | Ep: the epo has been informed by wipo that ep was designated in this application |
Ref document number: 14841264 Country of ref document: EP Kind code of ref document: A1 |
|
WWE | Wipo information: entry into national phase |
Ref document number: 14914233 Country of ref document: US |
|
NENP | Non-entry into the national phase |
Ref country code: DE |
|
REG | Reference to national code |
Ref country code: BR Ref legal event code: B01A Ref document number: 112016003892 Country of ref document: BR |
|
122 | Ep: pct application non-entry in european phase |
Ref document number: 14841264 Country of ref document: EP Kind code of ref document: A1 |
|
ENP | Entry into the national phase |
Ref document number: 112016003892 Country of ref document: BR Kind code of ref document: A2 Effective date: 20160223 |