CN115141099A - Production device and process of methyl methacrylate - Google Patents
Production device and process of methyl methacrylate Download PDFInfo
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- CN115141099A CN115141099A CN202110348107.5A CN202110348107A CN115141099A CN 115141099 A CN115141099 A CN 115141099A CN 202110348107 A CN202110348107 A CN 202110348107A CN 115141099 A CN115141099 A CN 115141099A
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- VVQNEPGJFQJSBK-UHFFFAOYSA-N Methyl methacrylate Chemical compound COC(=O)C(C)=C VVQNEPGJFQJSBK-UHFFFAOYSA-N 0.000 title claims abstract description 108
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 40
- 238000000034 method Methods 0.000 title claims description 26
- 230000008569 process Effects 0.000 title claims description 17
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims abstract description 308
- 125000002887 hydroxy group Chemical group [H]O* 0.000 claims abstract description 141
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 139
- 239000007789 gas Substances 0.000 claims abstract description 137
- 238000005882 aldol condensation reaction Methods 0.000 claims abstract description 132
- WSFSSNUMVMOOMR-UHFFFAOYSA-N Formaldehyde Chemical compound O=C WSFSSNUMVMOOMR-UHFFFAOYSA-N 0.000 claims abstract description 118
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 115
- 238000005886 esterification reaction Methods 0.000 claims abstract description 83
- 230000003647 oxidation Effects 0.000 claims abstract description 82
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 82
- 230000003197 catalytic effect Effects 0.000 claims abstract description 70
- 238000005336 cracking Methods 0.000 claims abstract description 66
- 230000032050 esterification Effects 0.000 claims abstract description 66
- 239000012495 reaction gas Substances 0.000 claims abstract description 50
- 238000006709 oxidative esterification reaction Methods 0.000 claims abstract description 47
- NBBJYMSMWIIQGU-UHFFFAOYSA-N Propionic aldehyde Chemical compound CCC=O NBBJYMSMWIIQGU-UHFFFAOYSA-N 0.000 claims description 108
- 239000000047 product Substances 0.000 claims description 100
- 239000001257 hydrogen Substances 0.000 claims description 76
- 229910052739 hydrogen Inorganic materials 0.000 claims description 76
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 74
- 229910002091 carbon monoxide Inorganic materials 0.000 claims description 74
- STNJBCKSHOAVAJ-UHFFFAOYSA-N Methacrolein Chemical compound CC(=C)C=O STNJBCKSHOAVAJ-UHFFFAOYSA-N 0.000 claims description 73
- 238000000605 extraction Methods 0.000 claims description 67
- 239000007795 chemical reaction product Substances 0.000 claims description 64
- 239000007791 liquid phase Substances 0.000 claims description 62
- ZTQSAGDEMFDKMZ-UHFFFAOYSA-N butyric aldehyde Natural products CCCC=O ZTQSAGDEMFDKMZ-UHFFFAOYSA-N 0.000 claims description 54
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 45
- 235000019256 formaldehyde Nutrition 0.000 claims description 41
- 239000012071 phase Substances 0.000 claims description 41
- 230000018044 dehydration Effects 0.000 claims description 34
- 238000006297 dehydration reaction Methods 0.000 claims description 34
- 150000002431 hydrogen Chemical class 0.000 claims description 31
- FUSUHKVFWTUUBE-UHFFFAOYSA-N buten-2-one Chemical compound CC(=O)C=C FUSUHKVFWTUUBE-UHFFFAOYSA-N 0.000 claims description 15
- 238000006243 chemical reaction Methods 0.000 claims description 15
- 238000001704 evaporation Methods 0.000 claims description 13
- 230000008020 evaporation Effects 0.000 claims description 13
- 238000000354 decomposition reaction Methods 0.000 claims description 12
- -1 hydroxyl compound Chemical class 0.000 claims description 8
- 239000012074 organic phase Substances 0.000 claims description 8
- 238000004064 recycling Methods 0.000 claims description 8
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 8
- 239000008346 aqueous phase Substances 0.000 claims description 6
- 239000000463 material Substances 0.000 claims description 5
- 229910001868 water Inorganic materials 0.000 claims description 5
- 239000003795 chemical substances by application Substances 0.000 claims description 3
- 230000002194 synthesizing effect Effects 0.000 claims description 2
- 239000003054 catalyst Substances 0.000 description 28
- 238000011084 recovery Methods 0.000 description 20
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 14
- 239000005977 Ethylene Substances 0.000 description 14
- 239000006227 byproduct Substances 0.000 description 11
- 239000002994 raw material Substances 0.000 description 9
- 238000006555 catalytic reaction Methods 0.000 description 7
- 239000002351 wastewater Substances 0.000 description 7
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 5
- 239000003570 air Substances 0.000 description 5
- WEVYAHXRMPXWCK-UHFFFAOYSA-N Acetonitrile Chemical compound CC#N WEVYAHXRMPXWCK-UHFFFAOYSA-N 0.000 description 3
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 3
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 3
- 238000012824 chemical production Methods 0.000 description 3
- 239000003245 coal Substances 0.000 description 3
- 229910001873 dinitrogen Inorganic materials 0.000 description 3
- 239000007792 gaseous phase Substances 0.000 description 3
- 238000002309 gasification Methods 0.000 description 3
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- HEDRZPFGACZZDS-UHFFFAOYSA-N Chloroform Chemical compound ClC(Cl)Cl HEDRZPFGACZZDS-UHFFFAOYSA-N 0.000 description 2
- KFZMGEQAYNKOFK-UHFFFAOYSA-N Isopropanol Chemical compound CC(C)O KFZMGEQAYNKOFK-UHFFFAOYSA-N 0.000 description 2
- XYFCBTPGUUZFHI-UHFFFAOYSA-N Phosphine Chemical compound P XYFCBTPGUUZFHI-UHFFFAOYSA-N 0.000 description 2
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 2
- 238000004523 catalytic cracking Methods 0.000 description 2
- 239000011248 coating agent Substances 0.000 description 2
- 238000000576 coating method Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- VLKZOEOYAKHREP-UHFFFAOYSA-N n-Hexane Chemical compound CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 1
- 239000004609 Impact Modifier Substances 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000001273 butane Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 239000013064 chemical raw material Substances 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 229920001577 copolymer Polymers 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 238000004043 dyeing Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 229940117927 ethylene oxide Drugs 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000002905 metal composite material Substances 0.000 description 1
- WSFSSNUMVMOOMR-NJFSPNSNSA-N methanone Chemical compound O=[14CH2] WSFSSNUMVMOOMR-NJFSPNSNSA-N 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 229910000073 phosphorus hydride Inorganic materials 0.000 description 1
- 229920003229 poly(methyl methacrylate) Polymers 0.000 description 1
- 239000004926 polymethyl methacrylate Substances 0.000 description 1
- 229920000915 polyvinyl chloride Polymers 0.000 description 1
- 239000004800 polyvinyl chloride Substances 0.000 description 1
- 238000007639 printing Methods 0.000 description 1
- 239000001294 propane Substances 0.000 description 1
- 230000001681 protective effect Effects 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 125000000383 tetramethylene group Chemical group [H]C([H])([*:1])C([H])([H])C([H])([H])C([H])([H])[*:2] 0.000 description 1
- 239000004753 textile Substances 0.000 description 1
- 229910052723 transition metal Inorganic materials 0.000 description 1
- 150000003624 transition metals Chemical class 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Images
Classifications
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C67/00—Preparation of carboxylic acid esters
- C07C67/36—Preparation of carboxylic acid esters by reaction with carbon monoxide or formates
- C07C67/38—Preparation of carboxylic acid esters by reaction with carbon monoxide or formates by addition to an unsaturated carbon-to-carbon bond
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/22—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of gaseous or liquid organic compounds
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B32/00—Carbon; Compounds thereof
- C01B32/40—Carbon monoxide
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C69/00—Esters of carboxylic acids; Esters of carbonic or haloformic acids
- C07C69/52—Esters of acyclic unsaturated carboxylic acids having the esterified carboxyl group bound to an acyclic carbon atom
- C07C69/533—Monocarboxylic acid esters having only one carbon-to-carbon double bond
- C07C69/54—Acrylic acid esters; Methacrylic acid esters
Abstract
The application provides a production device and a production process of methyl methacrylate, and belongs to the technical field of petrochemical industry. The device comprises: a methanol cracking unit, a hydroxyl synthesis unit, an aldol condensation unit and an oxidative esterification unit; one side of the methanol cracking unit is provided with a feed inlet for inputting methanol; the discharge hole of the methanol cracking unit is connected with the feed inlet of the hydroxyl synthesis unit, and the feed inlet of the hydroxyl synthesis unit is also used for being connected with the catalytic dry gas tank; the discharge hole of the hydroxyl synthesis unit is connected with the feed inlet of the aldol condensation unit, and the feed inlet of the aldol condensation unit is also used for being connected with the formaldehyde tank; the discharge hole of the aldol condensation unit is connected with the feed inlet of the oxidation esterification unit, and the feed inlet of the oxidation esterification unit is also used for being connected with a reaction gas tank. The device can be used for producing methyl methacrylate, and the production cost of methyl methacrylate can be effectively reduced.
Description
Technical Field
The application relates to the technical field of petrochemical industry, in particular to a production device and a production process of methyl methacrylate.
Background
Methyl methacrylate is an important chemical raw material, can be used for producing a plurality of industrial raw materials such as polymethyl methacrylate, polyvinyl chloride impact modifier, methyl methacrylate-styrene-butadiene copolymer, high-performance coating and the like, and is widely applied to various industries such as coating, electronic equipment, textile printing and dyeing, automobiles, medicine, buildings and the like, so how to efficiently produce methyl methacrylate is very important for the development of related industries
In the related technology, methyl methacrylate is mainly produced by an ethylene method, and the main raw materials for producing methyl methacrylate by the ethylene method are polymerization-grade ethylene and carbon monoxide; wherein, the polymer-grade ethylene is produced by adopting a cryogenic separation scheme, and the carbon monoxide is produced by adopting a coal gasification scheme. The production cost of the polymer-grade ethylene is high due to high investment and energy consumption when the cryogenic separation scheme is adopted to produce the polymer-grade ethylene; when the coal gasification scheme is adopted to produce the carbon monoxide, the scale is large, the raw materials are expensive, and the production cost of the carbon monoxide is higher, so that the production cost of the methyl methacrylate is higher due to the polymerization-grade ethylene and the carbon monoxide.
Disclosure of Invention
The embodiment of the application provides a production device and a production process of methyl methacrylate, which can reduce the production cost of methyl methacrylate. The technical scheme is as follows:
in one aspect, there is provided an apparatus for producing methyl methacrylate, the apparatus comprising: a methanol cracking unit, a hydroxyl synthesis unit, an aldol condensation unit and an oxidative esterification unit;
a feed inlet is formed in one side of the methanol cracking unit and used for inputting methanol;
the discharge hole of the methanol cracking unit is connected with the feed hole of the hydroxyl synthesis unit, the feed hole of the hydroxyl synthesis unit is also used for being connected with a catalytic dry gas tank, and the catalytic dry gas tank is used for inputting catalytic dry gas to the hydroxyl synthesis unit;
the discharge hole of the hydroxyl synthesis unit is connected with the feed inlet of the aldol condensation unit, the feed inlet of the aldol condensation unit is also used for being connected with a formaldehyde tank, and the formaldehyde tank is used for inputting formaldehyde into the aldol condensation unit;
the discharge hole of the aldol condensation unit is connected with the feed hole of the oxidation esterification unit, the feed hole of the oxidation esterification unit is also used for being connected with a reaction gas tank, and the reaction gas tank is used for inputting reaction gas into the oxidation esterification unit;
the methanol cracking unit is used for carrying out cracking decomposition reaction on the methanol to obtain carbon monoxide and hydrogen, and the carbon monoxide and the hydrogen are input into the hydroxyl synthesis unit;
the hydroxyl synthesis unit is used for receiving a hydroxyl compound with the mass ratio of 40% -45%: 10% -15%: 10% -15% of the catalytic dry gas, the carbon monoxide and the hydrogen, carrying out hydroxyl synthesis reaction on the catalytic dry gas, the carbon monoxide and the hydrogen to obtain propionaldehyde, and inputting the propionaldehyde into the aldol condensation unit;
the aldol condensation unit is used for receiving the following components in a mass ratio of 45-55%: performing aldol condensation reaction on 45-55% of the propionaldehyde and the formaldehyde to obtain methacrolein, and inputting the methacrolein into the oxidation esterification unit;
the oxidation esterification unit is used for receiving the following components in a mass ratio of 5% -15%: 30-40% of the methacrolein and the reaction gas, and carrying out oxidation esterification reaction on the methacrolein and the reaction gas to obtain the methyl methacrylate.
In one possible implementation, the hydroxyl synthesis unit comprises a hydroxyl synthesis reactor, a recycle gas compressor, a first flash tank, and a first rectification column;
the bottom end of the hydroxyl synthesis reactor is provided with a feed inlet, the feed inlet of the hydroxyl synthesis reactor is respectively connected with the discharge hole of the methanol cracking unit and the discharge hole of the circulating gas compressor, and the feed inlet of the hydroxyl synthesis reactor is also used for being connected with the catalytic dry gas tank;
a discharge hole is formed in the top end of the hydroxyl synthesis reactor, the discharge hole of the hydroxyl synthesis reactor is connected with a feed hole of the first flash tank, and the discharge hole of the first flash tank is respectively connected with a feed hole of the circulating gas compressor and a feed hole of the first rectifying tower;
the discharge hole of the first rectifying tower is connected with the feed inlet of the aldol condensation unit;
the hydroxyl synthesis reactor is used for receiving a hydroxyl compound with the mass ratio of 40% -45%: 10% -15%: 10% -15% of the catalytic dry gas, the carbon monoxide and the hydrogen, performing hydroxyl synthesis reaction on the catalytic dry gas, the carbon monoxide and the hydrogen to obtain a first reaction product, and inputting the first reaction product into the first flash tank;
the first flash tank is used for receiving the first reaction product, carrying out flash evaporation on the first reaction product to obtain a first gas-phase product and a first liquid-phase product, and respectively inputting the first gas-phase product and the first liquid-phase product into the circulating gas compressor and the first rectifying tower;
the recycle gas compressor is used for compressing the first gas phase product and inputting the compressed first gas phase product into the hydroxyl synthesis reactor for recycling;
and the first rectifying tower is used for rectifying the first liquid phase product to obtain propionaldehyde, and the propionaldehyde is input into the aldol condensation unit.
In one possible implementation, the aldol condensation unit comprises an aldol condensation reactor, a dehydration column, and a second rectification column;
a feed inlet is formed in the top end of the aldol condensation reactor, and the feed inlet of the aldol condensation reactor is respectively connected with the discharge port of the hydroxyl synthesis unit and the formaldehyde tank;
a discharge hole is formed in the bottom end of the aldol condensation reactor, the discharge hole of the aldol condensation reactor is connected with the feed hole of the dehydration tower, and the discharge hole of the dehydration tower is connected with the feed hole of the second rectification tower;
the discharge hole of the second rectifying tower is connected with the feed inlet of the oxidative esterification unit;
the aldol condensation reactor is used for receiving the following components in a mass ratio of 45-55%: performing aldol condensation reaction on 45-55% of the propionaldehyde and the formaldehyde to obtain a second reaction product, and inputting the second reaction product into the dehydration tower;
the dehydration tower is used for dehydrating the second reaction product to obtain mixed methacrolein, and the mixed methacrolein is input into the second rectifying tower;
the second rectifying tower is used for rectifying the mixed methacrolein to obtain methacrolein, and the methacrolein is input into the oxidative esterification unit.
In one possible implementation, the oxidative esterification unit comprises an oxidative esterification reactor, a second flash tank, an extraction column, and a third rectification column;
a feed inlet is formed in the top end of the oxidation esterification reactor, and the feed inlet of the oxidation esterification reactor is respectively connected with a discharge port of the aldol condensation unit and the reaction gas tank;
a discharge hole is formed in the bottom end of the oxidation esterification reactor, the discharge hole of the oxidation esterification reactor is connected with the feed hole of the second flash tank, the discharge hole of the second flash tank is connected with the feed hole of the extraction tower, and the discharge hole of the extraction tower is connected with the feed hole of the third rectification tower;
the oxidation esterification reactor is used for receiving the following components in a mass ratio of 5% -15%: 30% -40% of the methacrolein and the reaction gas, carrying out oxidation esterification reaction on the methacrolein and the reaction gas to obtain a third reaction product, and inputting the third reaction product into the second flash tank;
the second flash tank is used for carrying out flash evaporation on the third reaction product to obtain a second gas-phase product and a second liquid-phase product, emptying the second gas-phase product and inputting the second liquid-phase product into the extraction tower;
the extraction tower is used for receiving the second liquid-phase product, extracting the second liquid-phase product to obtain mixed methyl methacrylate, and inputting the mixed methyl methacrylate into the third rectifying tower;
and the third rectifying tower is used for rectifying the mixed methyl methacrylate to obtain the methyl methacrylate.
In another aspect, there is provided a process for producing methyl methacrylate, which is applied to the production apparatus described in any one of the above, the process comprising:
performing cracking decomposition reaction on the methanol through the methanol cracking unit to obtain the carbon monoxide and the hydrogen, and inputting the carbon monoxide and the hydrogen into the hydroxyl synthesis unit;
the hydroxyl group synthesis unit has a reception mass ratio of 40% to 45%:10% -15%: 10% -15% of the catalytic dry gas, the carbon monoxide and the hydrogen, carrying out hydroxyl synthesis reaction on the catalytic dry gas, the carbon monoxide and the hydrogen to obtain the propionaldehyde, and inputting the propionaldehyde into the aldol condensation unit;
the mass ratio of reception by the aldol condensation unit is 45% to 55%:45% -55% of the methyl aldehyde and the propionaldehyde are subjected to aldol condensation reaction to obtain the methyl acrolein, and the methyl acrolein is input into the oxidation esterification unit;
the receiving mass ratio is 5 to 15 percent through the oxidation esterification unit: 30 to 40 percent of the methacrolein and the reaction gas, and carrying out oxidation esterification reaction on the methacrolein and the reaction gas to obtain the methyl methacrylate.
In one possible implementation, the hydroxyl synthesis unit comprises a hydroxyl synthesis reactor, a recycle gas compressor, a first flash tank, and a first rectification column;
the bottom end of the hydroxyl synthesis reactor is provided with a feed inlet, the feed inlet of the hydroxyl synthesis reactor is respectively connected with the discharge hole of the methanol cracking unit and the discharge hole of the circulating gas compressor, and the feed inlet of the hydroxyl synthesis reactor is also used for being connected with the catalytic dry gas tank;
a discharge hole is formed in the top end of the hydroxyl synthesis reactor, the discharge hole of the hydroxyl synthesis reactor is connected with a feed hole of the first flash tank, and the discharge hole of the first flash tank is respectively connected with a feed hole of the circulating gas compressor and a feed hole of the first rectifying tower;
the discharge hole of the first rectifying tower is connected with the feed inlet of the aldol condensation unit;
the hydroxyl synthesis unit is used for synthesizing the hydroxyl groups, wherein the receiving mass ratio is 40-45%: 10% -15%: 10% -15% of the catalytic dry gas, the carbon monoxide and the hydrogen, performing a hydroxyl synthesis reaction on the catalytic dry gas, the carbon monoxide and the hydrogen to obtain the propionaldehyde, and inputting the propionaldehyde into the aldol condensation unit, wherein the method comprises the following steps of:
the hydroxyl synthesis reactor has a receiving mass ratio of 40-45%: 10% -15%: 10% -15% of the catalytic dry gas, the carbon monoxide and the hydrogen, performing hydroxyl synthesis reaction on the catalytic dry gas, the carbon monoxide and the hydrogen to obtain a first reaction product, and inputting the first reaction product into the first flash tank;
receiving the first reaction product through the first flash tank, carrying out flash evaporation on the first reaction product to obtain a first gas-phase product and a first liquid-phase product, and respectively inputting the first gas-phase product and the first liquid-phase product into the circulating gas compressor and the first rectifying tower;
compressing the first gas-phase product by the recycle gas compressor, and inputting the compressed first gas-phase product into the hydroxyl synthesis reactor for recycling;
and rectifying the first liquid phase product through the first rectifying tower to obtain propionaldehyde, and inputting the propionaldehyde into the aldol condensation unit.
In one possible implementation, the aldol condensation unit comprises an aldol condensation reactor, a dehydration column, and a second rectification column;
a feed inlet is formed in the top end of the aldol condensation reactor, and the feed inlet of the aldol condensation reactor is respectively connected with the discharge port of the hydroxyl synthesis unit and the formaldehyde tank;
a discharge hole is formed in the bottom end of the aldol condensation reactor, the discharge hole of the aldol condensation reactor is connected with the feed hole of the dehydration tower, and the discharge hole of the dehydration tower is connected with the feed hole of the second rectification tower;
the discharge hole of the second rectifying tower is connected with the feed inlet of the oxidative esterification unit;
the mass ratio of reception by the aldol condensation unit is 45-55%: 45% -55% of the methyl aldehyde and the propionaldehyde are subjected to aldol condensation reaction to obtain the methyl acrolein, and the methyl acrolein is input into the oxidation esterification unit, wherein the method comprises the following steps:
the mass ratio of the materials to be received by the aldol condensation reactor is 45-55%: performing aldol condensation reaction on 45-55% of the propionaldehyde and the formaldehyde to obtain a second reaction product, and inputting the second reaction product into the dehydration tower;
dehydrating the second reaction product through the dehydrating tower to obtain mixed methacrolein, and inputting the mixed methacrolein into the second rectifying tower;
and rectifying the mixed methacrolein through the second rectifying tower to obtain methacrolein, and inputting the methacrolein into the oxidative esterification unit.
In one possible implementation, the oxidative esterification unit comprises an oxidative esterification reactor, a second flash tank, an extraction column, and a third rectification column;
a feed inlet is formed in the top end of the oxidation esterification reactor, and the feed inlet of the oxidation esterification reactor is respectively connected with a discharge port of the aldol condensation unit and the reaction gas tank;
a discharge hole is formed in the bottom end of the oxidation esterification reactor, the discharge hole of the oxidation esterification reactor is connected with the feed hole of the second flash tank, the discharge hole of the second flash tank is connected with the feed hole of the extraction tower, and the discharge hole of the extraction tower is connected with the feed hole of the third rectification tower;
the receiving mass ratio of the oxidizing esterification unit is 5-15%: 30% to 40% of the methacrolein and the reaction gas, and subjecting the methacrolein and the reaction gas to an oxidative esterification reaction to obtain the methyl methacrylate, comprising:
the receiving mass ratio is 5 to 15 percent through the oxidation esterification reactor: 30% -40% of the methacrolein and the reaction gas, carrying out oxidation esterification reaction on the methacrolein and the reaction gas to obtain a third reaction product, and inputting the third reaction product into the second flash tank;
carrying out flash evaporation on the third reaction product through the second flash tank to obtain a second gas-phase product and a second liquid-phase product, emptying the second gas-phase product, and inputting the second liquid-phase product into the extraction tower;
receiving the second liquid-phase product through the extraction tower, extracting the second liquid-phase product to obtain mixed methyl methacrylate, and inputting the mixed methyl methacrylate into the third rectifying tower;
and rectifying the mixed methyl methacrylate by the third rectifying tower to obtain the methyl methacrylate.
In one possible implementation, the second liquid-phase product comprises an organic phase and an aqueous phase;
receiving the second liquid-phase product through the extraction column, and extracting the second liquid-phase product to obtain mixed methyl methacrylate, wherein the mixed methyl methacrylate comprises:
and (3) reversely contacting the second liquid-phase product with an extracting agent in the extraction tower through the extraction tower, so that the organic phase is separated from the aqueous phase, and the mixed methyl methacrylate is obtained.
In one possible implementation mode, the reaction temperature of the oxidative esterification reaction is 50-150 ℃, and the reaction pressure is 0.2-1.2MPa.
The technical scheme provided by the embodiment of the application has the beneficial effects that at least:
the embodiment of the application provides a production device of methyl methacrylate, on one hand, a methanol cracking unit can be used for carrying out cracking decomposition reaction on methanol to obtain carbon monoxide and hydrogen, and the methanol is cheap and easy to obtain, so that the production cost of the carbon monoxide and the hydrogen is reduced; on the other hand, the hydroxyl synthesis reaction, the aldol condensation reaction and the oxidative esterification reaction can be sequentially carried out on the carbon monoxide and the hydrogen obtained by the catalytic dry gas and the methanol cracking unit through the hydroxyl synthesis unit, the aldol condensation unit and the oxidative esterification unit to obtain the methyl methacrylate, and the catalytic dry gas is a byproduct of chemical production, so that the price is low and the methyl methacrylate is easily obtained, and the production cost is further reduced; therefore, the production cost of the methyl methacrylate can be effectively reduced by using the device to produce the methyl methacrylate.
Drawings
In order to more clearly illustrate the technical solutions in the embodiments of the present application, the drawings needed to be used in the description of the embodiments are briefly introduced below, and it is obvious that the drawings in the following description are only some embodiments of the present application, and it is obvious for those skilled in the art to obtain other drawings based on these drawings without creative efforts.
FIG. 1 is a block diagram of a methyl methacrylate production apparatus according to an embodiment of the present invention;
FIG. 2 is a block diagram of a methyl methacrylate production apparatus according to an embodiment of the present invention;
FIG. 3 is a flow chart of a process for producing methyl methacrylate according to the examples of the present application.
The reference numerals in the figures are denoted respectively by:
a 10-methanol cracking unit;
101-a methanol cracking reactor;
a 20-hydroxy synthesis unit;
201-hydroxyl synthesis reactor;
202-a recycle gas compressor;
203-a first flash tank;
204-a first rectification column;
205-a catalyst regenerator;
a 30-aldol condensation unit;
301-aldol condensation reactor;
302-a dehydration column;
303-a second rectification column;
a 40-oxidative esterification unit;
401-an oxidative esterification reactor;
402-a second flash tank;
403-an extraction column;
404-a third rectification column;
405-methanol recovery column.
Detailed Description
To make the objects, technical solutions and advantages of the present application more clear, embodiments of the present application will be described in further detail below with reference to the accompanying drawings.
The terms "first," "second," "third," and "fourth," etc. in the description and claims of this application and in the accompanying drawings are used for distinguishing between different objects and not for describing a particular order. Furthermore, the terms "comprising" and "having," as well as any variations thereof, are intended to cover non-exclusive inclusions. For example, a process, method, system, article, or apparatus that comprises a list of steps or elements is not limited to only those steps or elements listed, but may alternatively include other steps or elements not listed, or inherent to such process, method, article, or apparatus.
The embodiment of the application provides a production device of methyl methacrylate, and referring to fig. 1, the device comprises: a methanol cracking unit 10, a hydroxyl synthesis unit 20, an aldol condensation unit 30, and an oxidative esterification unit 40.
One side of the methanol cracking unit 10 is provided with a feed inlet for feeding methanol. The discharge port of the methanol cracking unit 10 is connected with the feed port of the hydroxyl synthesis unit 20, the feed port of the hydroxyl synthesis unit 20 is also used for being connected with a catalytic dry gas tank, and the catalytic dry gas tank is used for inputting catalytic dry gas to the hydroxyl synthesis unit 20. The discharge port of the hydroxyl synthesis unit 20 is connected with the feed port of the aldol condensation unit 30, and the feed port of the aldol condensation unit 30 is also used for being connected with a formaldehyde tank, and the formaldehyde tank is used for inputting formaldehyde into the aldol condensation unit 30. The discharge port of the aldol condensation unit 30 is connected with the feed port of the oxidation esterification unit 40, and the feed port of the oxidation esterification unit 40 is also used for being connected with a reaction gas tank, and the reaction gas tank is used for inputting reaction gas into the oxidation esterification unit 40.
And the methanol cracking unit 10 is used for performing cracking decomposition reaction on the methanol to obtain carbon monoxide and hydrogen, and inputting the carbon monoxide and the hydrogen into the hydroxyl synthesis unit 20. A hydroxyl synthesis unit 20 for receiving a hydroxyl compound having a mass ratio of 40% to 45%:10% -15%: 10% -15% of catalytic dry gas, carbon monoxide and hydrogen, carrying out hydroxyl synthesis reaction on the catalytic dry gas, the carbon monoxide and the hydrogen to obtain propionaldehyde, and inputting the propionaldehyde into an aldol condensation unit 30. An aldol condensation unit 30 for receiving: 45 to 55 percent of propionaldehyde and formaldehyde carry out aldol condensation reaction on the propionaldehyde and the formaldehyde to obtain methacrolein, and the methacrolein is input into the oxidation esterification unit 40. The oxidation esterification unit 40 is used for receiving the following components in a mass ratio of 5% -15%: 30 to 40 percent of methylacrolein and reaction gas, and carrying out oxidation esterification reaction on the methylacrolein and the reaction gas to obtain the methyl methacrylate.
The embodiment of the application provides a production device of methyl methacrylate, on one hand, the methanol cracking unit 10 can be used for cracking and decomposing methanol to obtain carbon monoxide and hydrogen, and the methanol is cheap and easy to obtain, so that the production cost of the carbon monoxide and the hydrogen is reduced; on the other hand, the hydroxyl synthesis reaction, the aldol condensation reaction and the oxidative esterification reaction can be sequentially performed on the catalytic dry gas and the carbon monoxide and the hydrogen obtained by the methanol cracking unit 10 through the hydroxyl synthesis unit 20, the aldol condensation unit 30 and the oxidative esterification unit 40 to obtain the methyl methacrylate, and the catalytic dry gas is a byproduct of chemical production, so that the catalytic dry gas is cheap and easy to obtain, and the production cost of the methyl methacrylate is reduced; therefore, the production cost of the methyl methacrylate can be effectively reduced by using the device to produce the methyl methacrylate.
Continuing to refer to fig. 1, a feed inlet is provided at one side of the methanol cracking unit 10 for feeding methanol; the discharge hole of the methanol cracking unit 10 is connected with the feed hole of the hydroxyl synthesis unit 20. And the methanol cracking unit 10 is used for performing cracking decomposition reaction on methanol to obtain carbon monoxide and hydrogen, and the carbon monoxide and the hydrogen are input into the hydroxyl synthesis unit 20.
Referring to fig. 2, the methanol cracking unit 10 includes a methanol cracking reactor 101, and a feed inlet is formed at one side of the methanol cracking reactor 101 for feeding methanol; the discharge port of the methanol cracking unit 10 comprises a top discharge port at the top end of the methanol cracking reactor 101 and a bottom discharge port at the bottom end of the methanol cracking reactor 101, and the top discharge port of the methanol cracking reactor 101 and the bottom discharge port of the methanol cracking reactor 101 are respectively connected with the feed port of the hydroxyl synthesis unit 20.
The methanol cracking reactor 101 is configured to perform cracking decomposition reaction on methanol to obtain a mixed gas of carbon monoxide and hydrogen, separate the mixed gas to obtain carbon monoxide and hydrogen, input the hydrogen into the hydroxyl synthesis unit 20 through a discharge port at a top end of the methanol cracking reactor 101, and input the carbon monoxide into the hydroxyl synthesis unit 20 through a discharge port at a bottom end of the methanol cracking reactor 101.
In a possible implementation manner, the top discharge port of the methanol cracking reactor 101 is further configured to be connected to a hydrogen tank, and the hydrogen tank is configured to receive the excess hydrogen discharged from the top discharge port of the methanol cracking reactor 101, so that the excess hydrogen can be used for producing other industrial raw materials.
Wherein the reaction temperature of the cracking decomposition reaction is 220-280 ℃, and the reaction pressure is 0.8-2.5Mpa.
In the embodiment of the application, methanol is used as a raw material to produce carbon monoxide and hydrogen through cracking decomposition, and the methanol is cheap and easy to obtain, so that the production cost of the carbon monoxide is effectively reduced compared with the traditional technology for producing the carbon monoxide through coal gasification.
With continued reference to fig. 1, the feed inlet of the hydroxyl synthesis unit 20 is connected to the discharge port of the methanol cracking unit 10 and the catalytic dry gas tank, respectively, and the discharge port of the hydroxyl synthesis unit 20 is connected to the feed inlet of the aldol condensation unit 30. A hydroxyl synthesis unit 20 for receiving a hydroxyl compound having a mass ratio of 40% to 45%:10% -15%: 10% -15% of catalytic dry gas, carbon monoxide and hydrogen, carrying out hydroxyl synthesis reaction on the catalytic dry gas, the carbon monoxide and the hydrogen to obtain propionaldehyde, and inputting the propionaldehyde into an aldol condensation unit 30.
With continued reference to fig. 2, the hydroxyl synthesis unit 20 includes a hydroxyl synthesis reactor 201, a recycle gas compressor 202, a first flash tank 203, and a first rectification column 204.
Wherein, the bottom of hydroxyl synthesis reactor 201 is equipped with the feed inlet, and the feed inlet of hydroxyl synthesis reactor 201 is connected with the discharge gate of methanol cracking unit 10 and the discharge gate of circulating gas compressor 202 respectively, and the feed inlet of hydroxyl synthesis reactor 201 still is used for being connected with the catalysis dry gas jar, and the catalysis dry gas jar is used for inputing catalysis dry gas to hydroxyl synthesis reactor 201. The top of the hydroxyl synthesis reactor 201 is provided with a discharge port, and the discharge port of the hydroxyl synthesis reactor 201 is connected with the feed port of the first flash tank 203.
Wherein, the feed inlet of the hydroxyl synthesis reactor 201 is respectively connected with the discharge outlet at the top end of the methanol cracking reactor 101 and the discharge outlet at the bottom end of the methanol cracking reactor 101.
Wherein, the catalysis dry gas in the catalysis dry gas jar is compressed gas, makes the volume of catalysis dry gas reduce like this, and has certain pressure, is convenient for save and carry.
A hydroxyl synthesis reactor 201 for receiving a hydroxyl compound with a mass ratio of 40% to 45%:10% -15%: 10 to 15 percent of catalytic dry gas, carbon monoxide and hydrogen, and carrying out hydroxyl synthesis reaction on the catalytic dry gas, the carbon monoxide and the hydrogen to obtain a first reaction product, and inputting the first reaction product into a first flash tank 203.
Wherein, the hydroxyl synthesis reactor 201 is filled with a hydroxyl synthesis catalyst, and the hydroxyl synthesis catalyst can be a complex compound of transition metal and organic phosphine; the hydroxyl synthesis reactor 201 is used for reacting the hydroxyl synthesis catalyst in a mass ratio of 40-45%: 10% -15%: carrying out hydroxyl synthesis reaction on 10-15% of catalytic dry gas, carbon monoxide and hydrogen to obtain a first reaction product; the content of the hydroxyl group synthesis catalyst may be set and changed as needed, and is not particularly limited herein.
Wherein the reaction temperature of the hydroxyl synthesis reaction is 50-150 ℃, and the reaction pressure is 1-2 Mpa.
The mass ratio of the catalytic dry gas to the carbon monoxide to the hydrogen can be set and changed according to the requirement; for example, the mass ratio of catalytic dry gas, carbon monoxide and hydrogen may be 43%:13%:13 percent.
Wherein, the components of the catalytic dry gas comprise ethylene, hydrogen, methane, ethane, propane, butane, butylene, pentane, carbon dioxide, oxygen, nitrogen, water, carbon monoxide and the like; ethylene in the catalytic dry gas is polymer-grade ethylene, the content of the ethylene is 15% -90%, and the content of hydrogen is 1% -5%; for example, referring to table 1, table 1 is a table of the composition of catalytic dry gas.
TABLE 1
The catalytic dry gas is from a catalytic cracking process, the catalytic cracking process is one of the most main secondary processing devices in China, the capacity is about 2.5 million tons/year, and more than 875 million tons/year of catalytic dry gas is produced every year according to 3.5 wt%. The ethylene content in the typical catalytic dry gas is 12-20wt%, and the hydrogen content in the typical catalytic dry gas is 1-3 wt%. At present, catalytic dry gas is mainly used as fuel, and high-value components such as ethylene, hydrogen and the like are not effectively utilized, so that great waste is caused. In the embodiment of the application, the method for producing the methyl methacrylate by developing and utilizing the ethylene and the hydrogen in the catalytic dry gas not only can fully utilize precious petroleum resources, but also can meet the domestic requirement on high-end chemical raw materials.
With continued reference to fig. 2, the feed inlet of the first flash tank 203 is connected to the feed outlet of the hydroxyl synthesis reactor 201, and the feed outlet of the first flash tank 203 is connected to the feed inlet of the recycle gas compressor 202 and the feed inlet of the first rectification column 204, respectively.
Wherein, the feed inlet setting of first flash tank 203 is in one side of first flash tank 203, and the discharge gate of first flash tank 203 includes the top discharge gate on first flash tank 203 top and the bottom discharge gate of first flash tank 203 bottom, and the top discharge gate of first flash tank 203 is connected with the feed inlet of circulating gas compressor 202, and the bottom discharge gate of first flash tank 203 is connected with the feed inlet of first rectifying column 204.
The first flash tank 203 is configured to receive the first reaction product, perform flash evaporation on the first reaction product to obtain a first gas-phase product and a first liquid-phase product, and input the first gas-phase product and the first liquid-phase product into the recycle gas compressor 202 and the first rectifying tower 204, respectively.
Wherein, first flash tank 203 inputs first gaseous phase result into circulating gas compressor 202 through the top discharge gate of first flash tank 203, inputs first liquid phase result into first rectifying column 204 through the bottom discharge gate of first flash tank 203, like this, because the weight of first liquid phase result is greater than first gaseous phase result, just can realize the high efficiency separation of first gaseous phase result and first liquid phase result.
With continued reference to fig. 2, the feed inlet of the recycle gas compressor 202 is connected to the first flash tank 203, and the discharge outlet of the recycle gas compressor 202 is connected to the hydroxyl synthesis reactor 201.
Wherein, the discharge port of the recycle gas compressor 202 is arranged at one side of the recycle gas compressor 202, and the feed port of the recycle gas compressor 202 is arranged at the other side of the recycle gas compressor 202.
And the recycle gas compressor 202 is used for compressing the first gas phase product and inputting the compressed first gas phase product into the hydroxyl synthesis reactor 201 for recycling.
Wherein the first gas phase product may be at least one of unreacted catalytic dry gas, carbon monoxide and hydrogen; in the embodiment of the present application, the unreacted gas is recycled to the hydroxyl group synthesis reactor 201 by the recycle gas compressor 202, so that the recycling of at least one of the catalytic dry gas, the carbon monoxide and the hydrogen is realized.
In another possible implementation manner, the discharge port of the recycle gas compressor 202 is further configured to be connected to an unreacted gas tank, and the unreacted gas tank is configured to receive the first gas-phase product discharged from the discharge port of the recycle gas compressor 202, so that the redundant first gas-phase product can be used for producing other industrial raw materials.
With continued reference to fig. 2, the feed inlet of the first rectification column 204 is connected with the discharge outlet of the first flash tank 203, and the discharge outlet of the first rectification column 204 is connected with the feed inlet of the aldol condensation unit 30.
Wherein, the feed inlet of the first rectifying tower 204 is arranged at one side of the first rectifying tower 204. The discharge port of the first rectifying tower 204 comprises a top discharge port at the top end of the first rectifying tower 204 and a bottom discharge port at the bottom end of the first rectifying tower 204, and the top discharge port of the first rectifying tower 204 is connected with the feed port of the aldol condensation unit 30.
With continued reference to fig. 2, the hydroxyl synthesis unit 20 further comprises a catalyst regenerator 205, the outlet of the bottom end of the first rectification column 204 is connected with the inlet of the catalyst regenerator 205, and the outlet of the catalyst regenerator 205 is connected with the inlet of the hydroxyl synthesis reactor 201. The inlet of the catalyst regenerator 205 is disposed at one side of the catalyst regenerator 205 and the outlet of the catalyst regenerator 205 is disposed at the other side of the catalyst regenerator 205.
The first rectifying tower 204 is configured to rectify the first liquid-phase product to obtain propionaldehyde, and input the propionaldehyde to the aldol condensation unit 30. The first rectifying tower 204 is further configured to rectify the first liquid-phase product to obtain a mixed catalyst, and the mixed catalyst is input to the catalyst regenerator 205. And the catalyst regenerator is used for regenerating the mixed catalyst to obtain the catalyst, and inputting the catalyst into the hydroxyl reaction synthesizer, so that the cyclic utilization of the catalyst is realized.
In the embodiment of the application, the hydroxyl synthesis unit 20 realizes that the catalytic dry gas, the carbon monoxide and the hydrogen are subjected to hydroxyl synthesis reaction, flash evaporation and rectification in sequence to obtain propionaldehyde, and the purity of the propionaldehyde is improved.
With continued reference to fig. 1, the feed inlet of the aldol condensation unit 30 is connected to the discharge outlet of the hydroxyl synthesis unit 20 and the formaldehyde tank, respectively, and the discharge outlet of the aldol condensation unit 30 is connected to the oxidative esterification unit 40; an aldol condensation unit 30 for receiving: 45 to 55 percent of propionaldehyde and formaldehyde carry out aldol condensation reaction on the propionaldehyde and the formaldehyde to obtain methacrolein, and the methacrolein is input into the oxidation esterification unit 40.
With continued reference to fig. 2, aldol condensation unit 30 comprises an aldol condensation reactor 301, a dehydration column 302 and a second rectification column 303.
Wherein, the top end of the aldol condensation reactor 301 is provided with a feed inlet, the feed inlet of the aldol condensation reactor 301 is respectively connected with the discharge port of the hydroxyl synthesis unit 20 and a formaldehyde tank, and the formaldehyde tank is used for inputting formaldehyde into the aldol condensation reactor 301. The bottom end of the aldol condensation reactor 301 is provided with a discharge port, and the discharge port of the aldol condensation reactor 301 is connected with the feed port of the dehydration tower 302.
Wherein, the feed inlet of the aldol condensation reactor 301 is connected with the discharge outlet at the top end of the first rectifying tower 204 of the hydroxyl synthesis unit 20.
Wherein, the catalysis dry gas in the formaldehyde jar is compressed gas, makes the volume of formaldehyde reduce like this, and has certain pressure, is convenient for store and transport.
The aldol condensation reactor 301 is used for receiving the following components in a mass ratio of 45-55%: 45% -55% of propionaldehyde and formaldehyde are subjected to aldol condensation reaction to obtain a second reaction product, and the second reaction product is input into the dehydration tower 302.
Wherein, the aldol condensation reactor 301 is filled with an aldol condensation catalyst which can be a heterogeneous solid base catalyst; an aldol condensation reactor 301 for reacting, under the action of an aldol condensation catalyst, a catalyst having a mass ratio of 45% to 55%: carrying out aldol condensation reaction on 45-55% of propionaldehyde and formaldehyde to obtain a second reaction product; the content of the aldol condensation catalyst may be set and changed as needed, and is not particularly limited.
Wherein the reaction temperature of the aldol condensation reaction is 100-200 ℃, and the reaction pressure is 3-7Mpa.
The mass ratio of the propionaldehyde to the formaldehyde can be set and changed according to requirements; for example, the mass ratio of propionaldehyde to formaldehyde may be 50%:50 percent.
With continued reference to fig. 2, the feed inlet of the dehydration column 302 is connected with the discharge outlet of the aldol condensation reactor 301, and the discharge outlet of the dehydration column 302 is connected with the feed inlet of the second rectification column 303.
Wherein, the feed inlet setting of dehydration tower 302 is in one side of dehydration tower 302, and the discharge gate of dehydration tower 302 includes the top discharge gate on dehydration tower 302 top and the bottom feed inlet of dehydration tower 302 bottom, and the top discharge gate of dehydration tower 302 is connected with the feed inlet of second rectifying column 303, and the bottom discharge gate of dehydration tower 302 is used for being connected with the waste water tank, and the waste water tank is used for receiving dehydration tower 302 exhaust waste water.
And a dehydrating tower 302 for dehydrating the second reaction product to obtain mixed methacrolein, and inputting the mixed methacrolein into a second rectifying tower 303.
Wherein, the mixed methacrolein is crude methacrolein, and the mixed methacrolein comprises methacrolein and heavy components.
With continued reference to fig. 2, the feed inlet of the second rectifying tower 303 is connected with the discharge outlet of the dehydrating tower 302, and the discharge outlet of the second rectifying tower 303 is connected with the feed inlet of the oxidative esterification unit 40.
Wherein, the feed inlet setting of second rectifying column 303 is in one side of second rectifying column 303, and the discharge gate of second rectifying column 303 includes the top discharge gate and the bottom discharge gate of second rectifying column 303, and the top discharge gate of second rectifying column 303 is connected with the feed inlet of oxidation esterification unit 40, and the bottom discharge gate and the heavy ends jar of second rectifying column 303 are connected, and the heavy ends jar is used for receiving the heavy ends of second rectifying column 303 discharge.
A second rectifying tower 303, configured to rectify the mixed methacrolein to obtain methacrolein, and input the methacrolein into the oxidative esterification unit 40; the second rectifying tower 303 is further configured to rectify the mixed methacrolein to obtain a heavy component, and the heavy component is input to the heavy component tank.
In the embodiment of the application, by providing the second rectifying tower 303, the mixed methacrolein is rectified, and therefore methacrolein is obtained.
In the embodiment of the application, the aldol condensation reaction, the dehydration and the rectification of propionaldehyde and formaldehyde are sequentially performed by the aldol condensation unit 30, so that the methacrolein is obtained, and the purity of the methacrolein is improved.
With continued reference to fig. 1, the feed inlets of the oxidative esterification unit 40 are respectively connected with the discharge outlet of the aldol condensation unit 30 and the reaction gas tank; the oxidation esterification unit 40 is used for receiving the following components in a mass ratio of 5% -15%: 30 to 40 percent of methylacrolein and reaction gas, and carrying out oxidation esterification reaction on the methylacrolein and the reaction gas to obtain the methyl methacrylate.
With continued reference to fig. 2, oxidative esterification unit 40 includes oxidative esterification reactor 401, second flash drum 402, extraction column 403, and third rectification column 404.
Wherein, the top end of the oxidation esterification reactor 401 is provided with a feed inlet, the feed inlet of the oxidation esterification reactor 401 is respectively connected with the discharge port of the aldol condensation unit 30 and a reaction gas tank, and the reaction gas tank is used for inputting reaction gas into the oxidation esterification reactor 401; the bottom end of the oxidation esterification reactor 401 is provided with a discharge hole, and the discharge hole of the oxidation esterification reactor 401 is connected with the feed inlet of the second flash tank 402.
Wherein, the feed inlet of the oxidation esterification reactor 401 is connected with the discharge outlet at the top end of the second rectifying tower 303 of the aldol condensation unit 30.
Wherein, the reaction gas tank comprises a methanol tank and an air tank, which are respectively used for inputting methanol and air to the feed inlet of the oxidation esterification reactor 401. The mass ratio of the methanol and the air can be set and changed according to the requirement; for example, the mass ratio of methanol to air is 10%:23 percent.
In another possible implementation manner, the feed inlet of the oxidative esterification reactor 401 is further used for connecting with a shielding gas tank, and the shielding gas tank is used for inputting shielding gas into the oxidative esterification reactor 401.
Wherein the protective gas tank comprises a water vapor tank and a nitrogen gas tank, which are respectively used for inputting water vapor and nitrogen gas to the feed inlet of the oxidation esterification reactor 401. The mass ratio of water vapor and nitrogen gas can be set and changed as required.
The oxidation esterification reactor 401 is used for receiving a mixture of the following components in a mass ratio of 5% -15%: 30% -40% of methacrolein and reaction gas, and carrying out oxidation esterification reaction on the methacrolein and the reaction gas to obtain a third reaction product, and inputting the third reaction product into the second flash tank 402.
Wherein, the oxidation esterification reactor 401 is filled with oxidation esterification catalyst, which can be heterogeneous metal composite oxide catalyst; the oxidation esterification reactor 401 is used for mixing 5-15% of: carrying out oxidation esterification reaction on 30-40% of methacrolein and reaction gas to obtain a third reaction product; the content of the oxidative esterification catalyst may be set and changed as needed, and is not particularly limited herein.
Wherein the reaction temperature of the oxidation esterification reaction is 50-150 ℃, and the reaction pressure is 0.2-1.2Mpa.
With continued reference to fig. 2, the feed inlet of the second flash tank 402 is connected to the discharge outlet of the oxidative esterification reactor 401, and the discharge outlet of the second flash tank 402 is connected to the feed inlet of the extraction column 403.
Wherein the feed inlet of the second flash tank 402 is arranged at one side of the second flash tank 402; the discharge ports of the second flash tank 402 comprise a top feed port at the top end of the second flash tank 402 and a bottom discharge port at the bottom end of the second flash tank 402; the discharge port at the top end of the second flash tank 402 is used for being connected with a flare system, the flare system is used for emptying gas, and the discharge port at the bottom end of the second flash tank 402 is connected with the feed port of the extraction tower 403.
And a second flash tank 402, configured to flash-evaporate the third reaction product to obtain a second gas-phase product and a second liquid-phase product, and empty the second gas-phase product and input the second liquid-phase product into the extraction tower 403.
With continued reference to fig. 2, the feed inlet of the extraction column 403 is connected to the feed outlet of the second flash drum 402, and the feed outlet of the extraction column 403 is connected to the feed inlet of the third rectification column 404.
The feed inlets of the extraction tower 403 include an upper feed inlet at the upper end of the extraction tower 403 and a lower feed inlet at the lower end of the extraction tower 403, the upper feed inlet of the extraction tower 403 is connected with the bottom feed inlet of the second flash tank 402, the lower feed inlet of the extraction tower 403 is used for connecting with an extractant tank, and the extractant tank is used for inputting an extractant into the extraction tower 403.
Wherein, the discharge gate of extraction column 403 includes the top discharge gate at the top of extraction column 403 and the bottom discharge gate of extraction column 403 bottom, and the top discharge gate of extraction column 403 is connected with third rectifying column 404. With continued reference to fig. 2, oxidative esterification unit 40 further comprises a methanol recovery column 405, and the outlet at the bottom end of extraction column 403 is connected to the inlet of methanol recovery column 405. The lower end feed inlet of the extraction tower 403 comprises a lower end feed inlet at one side of the extraction tower 403 and a lower end feed inlet at the other side of the extraction tower 403, the lower end feed inlet at one side of the extraction tower 403 is used for being connected with an extractant tank, and the lower end feed inlet at the other side of the extractant is connected with a discharge outlet of the methanol recovery tower 405.
The extraction tower 403 is configured to receive the second liquid-phase product, extract the second liquid-phase product to obtain mixed methyl methacrylate, and input the mixed methyl methacrylate into the third rectification tower 404; the extraction tower 403 is further configured to extract the second liquid-phase product to obtain a mixed extractant, and the mixed extractant is input to the methanol recovery tower 405.
Wherein the mixed methyl methacrylate is crude methyl methacrylate, including extractant, methyl methacrylate and other by-products.
Wherein the second liquid-phase product comprises an organic phase and an aqueous phase; and the extraction tower 403 is used for reversely contacting the second liquid-phase product with the extractant in the extraction tower 403, so that an organic phase is separated from the aqueous phase, and mixed methyl methacrylate is obtained.
In this application embodiment, through setting up extraction column 403, with the second liquid phase product from the input of the upper end feed inlet of extraction column 403, with the extractant from the input of the lower extreme feed inlet of extraction column 403, realized the reverse contact of second liquid phase product with the extractant, increased area of contact for can be to the more thorough of second liquid phase product extraction.
With continued reference to fig. 2, the feed inlet of the methanol recovery tower 405 is connected to the discharge outlet of the extraction tower 403, the discharge outlet of the methanol recovery tower 405 is connected to the feed inlet of the extraction tower 403 and the feed inlet of the oxidative esterification reaction reactor, respectively, and the methanol recovery tower 405 is further configured to be connected to a wastewater tank, and the wastewater tank is configured to receive wastewater discharged from the methanol recovery tower 405.
Wherein, the feed inlet of the methanol recovery tower 405 is arranged at one side of the methanol recovery tower 405, and the feed inlet of the methanol recovery tower 405 is connected with the discharge outlet at the bottom end of the extraction tower 403. The discharge port of the methanol recovery tower 405 comprises an upper end discharge port at the upper end of the methanol recovery tower 405, a top end discharge port at the top end of the methanol recovery tower 405 and a bottom end discharge port at the bottom end of the methanol recovery tower 405, the upper end discharge port of the methanol recovery tower 405 is connected with the lower end feed port at the other side of the extraction tower 403, the top end discharge port of the methanol recovery tower 405 is connected with the feed port of the oxidation esterification reactor 401, and the bottom end discharge port of the methanol recovery tower 405 is connected with the wastewater tank.
And the methanol recovery tower 405 is configured to receive the mixed extractant, recover the mixed extractant to obtain the extractant and methanol, and input the extractant and the methanol into the extraction tower 403 and the oxidation esterification reactor 401 respectively for recycling.
Wherein the extractant can be at least one or more of water, methanol, ethanol, isopropanol, acetonitrile, n-hexane, chloroform, and toluene.
With continued reference to fig. 2, the feed inlet of the third rectification column 404 is connected with the discharge outlet of the extraction column 403; the feed inlet of the third rectifying tower 404 is arranged at one side of the third rectifying tower 404, and the feed inlet of the third rectifying tower 404 is connected with the discharge outlet at the top end of the extraction tower 403.
With continued reference to fig. 2, the top end and the bottom end of the third rectifying tower 404 are respectively provided with a discharge port, the discharge port of the third rectifying tower 404 is respectively connected with a byproduct tank and a methyl methacrylate tank, the byproduct tank is used for receiving the byproducts discharged from the third rectifying tower 404, and the methyl methacrylate tank is used for receiving the methyl methacrylate discharged from the third rectifying tower 404. The discharge port of the third rectifying tower 404 comprises a top discharge port at the top end of the third rectifying tower 404 and a bottom discharge port at the bottom end of the third rectifying tower 404, the top discharge port of the third rectifying tower 404 is connected with the byproduct tank, and the bottom discharge port of the third rectifying tower 404 is connected with the methyl methacrylate tank.
A third rectifying tower 404, configured to rectify the mixed methyl methacrylate to obtain methyl methacrylate; the third rectifying tower 404 is further configured to rectify the methyl methacrylate to obtain a byproduct, and the byproduct is input into the byproduct tank and the methyl methacrylate is input into the methyl methacrylate tank.
In the embodiment of the application, the third rectifying tower 404 is arranged to rectify the mixed methyl methacrylate to obtain the methyl methacrylate, so that the purity of the methyl methacrylate is improved.
In the embodiment of the application, the oxidative esterification reaction, the flash evaporation and the rectification of the methacrolein and the reaction gas are realized through the oxidative esterification unit 40, so that the methyl methacrylate is obtained, and the purity of the methyl methacrylate is improved.
Referring to table 2, table 2 is a material balance table for producing methyl methacrylate provided in the examples of the present application; the production raw materials comprise catalytic dry gas, formaldehyde, methanol and air, the products comprise fuel gas, hydrogen, methyl methacrylate and loss substances, and the quality of the production raw materials is the same as that of the products, so that the material balance before and after production is met.
TABLE 2
The embodiment of the application provides a production device of methyl methacrylate, on one hand, the methanol cracking unit 10 can be used for cracking and decomposing methanol to obtain carbon monoxide and hydrogen, and the methanol is cheap and easy to obtain, so that the production cost of the carbon monoxide and the hydrogen is reduced; on the other hand, the hydroxyl synthesis reaction, the aldol condensation reaction and the oxidative esterification reaction can be sequentially performed on the catalytic dry gas and the carbon monoxide and the hydrogen obtained by the methanol cracking unit 10 through the hydroxyl synthesis unit 20, the aldol condensation unit 30 and the oxidative esterification unit 40 to obtain the methyl methacrylate, and the catalytic dry gas is a byproduct of chemical production, so that the catalytic dry gas is cheap and easy to obtain, and the production cost of the methyl methacrylate is reduced; therefore, the production cost of the methyl methacrylate can be effectively reduced by using the device to produce the methyl methacrylate.
The embodiment of the application provides a production process of methyl methacrylate, and referring to fig. 3, the process comprises the following steps:
step 301: and (2) carrying out cracking decomposition reaction on the methanol by a methanol cracking unit to obtain carbon monoxide and hydrogen, and inputting the carbon monoxide and the hydrogen into a hydroxyl synthesis unit.
Step 302: the hydroxyl synthesis unit is used for receiving the signals with the mass ratio of 40-45%: 10% -15%: 10 to 15 percent of catalytic dry gas, carbon monoxide and hydrogen, carrying out hydroxyl synthesis reaction on the catalytic dry gas, the carbon monoxide and the hydrogen to obtain propionaldehyde, and inputting the propionaldehyde into an aldol condensation unit.
This step can be achieved by the following steps (1) to (4):
(1) The hydroxyl synthesis reactor is used for receiving the hydroxyl synthesis reaction product with the mass ratio of 40-45%: 10% -15%: 10% -15% of catalytic dry gas, carbon monoxide and hydrogen, carrying out hydroxyl synthesis reaction on the catalytic dry gas, the carbon monoxide and the hydrogen to obtain a first reaction product, and inputting the first reaction product into a first flash tank.
(2) And receiving the first reaction product through a first flash tank, carrying out flash evaporation on the first reaction product to obtain a first gas-phase product and a first liquid-phase product, and respectively inputting the first gas-phase product and the first liquid-phase product into a circulating gas compressor and a first rectifying tower.
(3) And compressing the first gas-phase product by a recycle gas compressor, and inputting the compressed first gas-phase product into a hydroxyl synthesis reactor for recycling.
(4) And rectifying the first liquid phase product through a first rectifying tower to obtain propionaldehyde, and inputting the propionaldehyde into an aldol condensation unit.
Step 303: the mass ratio of the materials received by an aldol condensation unit is 45-55%: propionaldehyde and formaldehyde account for 45-55%, the propionaldehyde and formaldehyde carry on the aldol condensation reaction to get methacrolein, input methacrolein into the unit of oxidation esterification.
This step can be realized by the following steps (1) to (3):
(1) Through an aldol condensation reactor, the mass ratio of receiving is 45-55%: and (2) performing aldol condensation reaction on 45-55% of propionaldehyde and formaldehyde to obtain a second reaction product, and inputting the second reaction product into a dehydration tower.
(2) And dehydrating the second reaction product through a dehydrating tower to obtain mixed methacrolein, and inputting the mixed methacrolein into a second rectifying tower.
(3) And (3) rectifying the mixed methacrolein by using a second rectifying tower to obtain methacrolein, and inputting the methacrolein into the oxidative esterification unit.
Step 304: the receiving mass ratio is 5 to 15 percent through an oxidation esterification unit: 30 to 40 percent of methylacrolein and reaction gas, and carrying out oxidation esterification reaction on the methylacrolein and the reaction gas to obtain the methyl methacrylate.
This step can be achieved by the following steps (1) to (4):
(1) The receiving mass ratio is 5 to 15 percent through an oxidation esterification reactor: 30 to 40 percent of methylacrolein and reaction gas are subjected to oxidation esterification reaction to obtain a third reaction product, and the third reaction product is input into a second flash tank.
Wherein the reaction temperature of the oxidation esterification reaction is 50-150 ℃, and the reaction pressure is 0.2-1.2Mpa.
(2) And (3) carrying out flash evaporation on the third reaction product through a second flash tank to obtain a second gas-phase product and a second liquid-phase product, emptying the second gas-phase product, and inputting the second liquid-phase product into the extraction tower.
(3) And receiving the second liquid-phase product through the extraction tower, extracting the second liquid-phase product to obtain mixed methyl methacrylate, and inputting the mixed methyl methacrylate into a third rectifying tower.
Wherein the second liquid-phase product comprises an organic phase and an aqueous phase; and (3) reversely contacting the second liquid-phase product with an extracting agent in the extraction tower through the extraction tower, so that an organic phase is separated from the water phase, and the mixed methyl methacrylate is obtained.
(4) And (3) rectifying the mixed methyl methacrylate by a third rectifying tower to obtain the methyl methacrylate.
The embodiment of the application provides a production method of methyl methacrylate, on one hand, the method can carry out cracking decomposition reaction on methanol through a methanol cracking unit to obtain carbon monoxide and hydrogen, and the production cost of the carbon monoxide and the hydrogen is reduced because the methanol is cheap and easy to obtain; on the other hand, the method can sequentially carry out hydroxyl synthesis reaction, aldol condensation reaction and oxidation esterification reaction on the catalytic dry gas and the carbon monoxide and the hydrogen obtained by the methanol cracking unit through a hydroxyl synthesis unit, an aldol condensation unit and an oxidation esterification unit to obtain the methyl methacrylate; therefore, the method for producing the methyl methacrylate can effectively reduce the production cost of the methyl methacrylate.
The above description is only exemplary of the present application and should not be taken as limiting, as any modification, equivalent replacement, or improvement made within the spirit and principle of the present application should be included in the protection scope of the present application.
Claims (10)
1. An apparatus for producing methyl methacrylate, characterized in that the apparatus comprises: a methanol cracking unit, a hydroxyl synthesis unit, an aldol condensation unit and an oxidative esterification unit;
a feed inlet is formed in one side of the methanol cracking unit and used for inputting methanol;
the discharge hole of the methanol cracking unit is connected with the feed inlet of the hydroxyl synthesis unit, the feed inlet of the hydroxyl synthesis unit is also used for being connected with a catalytic dry gas tank, and the catalytic dry gas tank is used for inputting catalytic dry gas to the hydroxyl synthesis unit;
the discharge hole of the hydroxyl synthesis unit is connected with the feed inlet of the aldol condensation unit, the feed inlet of the aldol condensation unit is also used for being connected with a formaldehyde tank, and the formaldehyde tank is used for inputting formaldehyde into the aldol condensation unit;
the discharge hole of the aldol condensation unit is connected with the feed hole of the oxidation esterification unit, the feed hole of the oxidation esterification unit is also used for being connected with a reaction gas tank, and the reaction gas tank is used for inputting reaction gas into the oxidation esterification unit;
the methanol cracking unit is used for carrying out cracking decomposition reaction on the methanol to obtain carbon monoxide and hydrogen, and the carbon monoxide and the hydrogen are input into the hydroxyl synthesis unit;
the hydroxyl synthesis unit is used for receiving the hydroxyl with the mass ratio of 40% -45%: 10% -15%: 10% -15% of the catalytic dry gas, the carbon monoxide and the hydrogen, carrying out hydroxyl synthesis reaction on the catalytic dry gas, the carbon monoxide and the hydrogen to obtain propionaldehyde, and inputting the propionaldehyde into the aldol condensation unit;
the aldol condensation unit is used for receiving the following components in a mass ratio of 45-55%: performing aldol condensation reaction on 45-55% of the propionaldehyde and the formaldehyde to obtain methacrolein, and inputting the methacrolein into the oxidation esterification unit;
the oxidation esterification unit is used for receiving the following components in a mass ratio of 5% -15%: 30 to 40 percent of the methacrolein and the reaction gas, and carrying out oxidation esterification reaction on the methacrolein and the reaction gas to obtain the methyl methacrylate.
2. The apparatus for producing methyl methacrylate according to claim 1, wherein the hydroxyl group synthesis unit comprises a hydroxyl group synthesis reactor, a recycle gas compressor, a first flash tank and a first rectification column;
the bottom end of the hydroxyl synthesis reactor is provided with a feed inlet, the feed inlet of the hydroxyl synthesis reactor is respectively connected with the discharge hole of the methanol cracking unit and the discharge hole of the circulating gas compressor, and the feed inlet of the hydroxyl synthesis reactor is also used for being connected with the catalytic dry gas tank;
a discharge hole is formed in the top end of the hydroxyl synthesis reactor, the discharge hole of the hydroxyl synthesis reactor is connected with a feed hole of the first flash tank, and the discharge hole of the first flash tank is respectively connected with a feed hole of the circulating gas compressor and a feed hole of the first rectifying tower;
the discharge hole of the first rectifying tower is connected with the feed inlet of the aldol condensation unit;
the hydroxyl synthesis reactor is used for receiving a hydroxyl compound with the mass ratio of 40% -45%: 10% -15%: 10% -15% of the catalytic dry gas, the carbon monoxide and the hydrogen, performing hydroxyl synthesis reaction on the catalytic dry gas, the carbon monoxide and the hydrogen to obtain a first reaction product, and inputting the first reaction product into the first flash tank;
the first flash tank is used for receiving the first reaction product, carrying out flash evaporation on the first reaction product to obtain a first gas-phase product and a first liquid-phase product, and respectively inputting the first gas-phase product and the first liquid-phase product into the circulating gas compressor and the first rectifying tower;
the recycle gas compressor is used for compressing the first gas phase product and inputting the compressed first gas phase product into the hydroxyl synthesis reactor for recycling;
and the first rectifying tower is used for rectifying the first liquid phase product to obtain propionaldehyde, and the propionaldehyde is input into the aldol condensation unit.
3. The apparatus for producing methyl methacrylate according to claim 1, wherein the aldol condensation unit comprises an aldol condensation reactor, a dehydration column, and a second rectification column;
a feed inlet is formed in the top end of the aldol condensation reactor, and the feed inlet of the aldol condensation reactor is respectively connected with the discharge port of the hydroxyl synthesis unit and the formaldehyde tank;
a discharge hole is formed in the bottom end of the aldol condensation reactor, the discharge hole of the aldol condensation reactor is connected with the feed hole of the dehydration tower, and the discharge hole of the dehydration tower is connected with the feed hole of the second rectification tower;
the discharge hole of the second rectifying tower is connected with the feed inlet of the oxidative esterification unit;
the aldol condensation reactor is used for receiving the following components in a mass ratio of 45-55%: performing aldol condensation reaction on 45-55% of the propionaldehyde and the formaldehyde to obtain a second reaction product, and inputting the second reaction product into the dehydration tower;
the dehydration tower is used for dehydrating the second reaction product to obtain mixed methacrolein, and the mixed methacrolein is input into the second rectifying tower;
the second rectifying tower is used for rectifying the mixed methacrolein to obtain methacrolein, and the methacrolein is input into the oxidative esterification unit.
4. The apparatus for producing methyl methacrylate according to claim 1, wherein the oxidative esterification unit comprises an oxidative esterification reactor, a second flash tank, an extraction column, and a third rectification column;
a feed inlet is formed in the top end of the oxidation esterification reactor, and the feed inlet of the oxidation esterification reactor is respectively connected with a discharge port of the aldol condensation unit and the reaction gas tank;
a discharge hole is formed in the bottom end of the oxidation esterification reactor, the discharge hole of the oxidation esterification reactor is connected with a feed hole of the second flash tank, the discharge hole of the second flash tank is connected with a feed hole of the extraction tower, and the discharge hole of the extraction tower is connected with a feed hole of the third rectification tower;
the oxidation esterification reactor is used for receiving the following components in a mass ratio of 5% -15%: 30% -40% of the methacrolein and the reaction gas, carrying out oxidation esterification reaction on the methacrolein and the reaction gas to obtain a third reaction product, and inputting the third reaction product into the second flash tank;
the second flash tank is used for carrying out flash evaporation on the third reaction product to obtain a second gas-phase product and a second liquid-phase product, emptying the second gas-phase product and inputting the second liquid-phase product into the extraction tower;
the extraction tower is used for receiving the second liquid-phase product, extracting the second liquid-phase product to obtain mixed methyl methacrylate, and inputting the mixed methyl methacrylate into the third rectifying tower;
and the third rectifying tower is used for rectifying the mixed methyl methacrylate to obtain the methyl methacrylate.
5. A process for producing methyl methacrylate, which is applied to the production apparatus according to any one of claims 1 to 4, the process comprising:
performing cracking decomposition reaction on the methanol through the methanol cracking unit to obtain the carbon monoxide and the hydrogen, and inputting the carbon monoxide and the hydrogen into the hydroxyl synthesis unit;
the hydroxyl group synthesis unit has a reception mass ratio of 40% to 45%:10% -15%: 10% -15% of the catalytic dry gas, the carbon monoxide and the hydrogen, carrying out hydroxyl synthesis reaction on the catalytic dry gas, the carbon monoxide and the hydrogen to obtain the propionaldehyde, and inputting the propionaldehyde into the aldol condensation unit;
the mass ratio of reception by the aldol condensation unit is 45 to 55%:45% -55% of the methyl aldehyde and the propionaldehyde are subjected to aldol condensation reaction to obtain the methyl acrolein, and the methyl acrolein is input into the oxidation esterification unit;
the receiving mass ratio is 5 to 15 percent through the oxidation esterification unit: 30-40% of the methacrolein and the reaction gas, and carrying out oxidation esterification reaction on the methacrolein and the reaction gas to obtain the methyl methacrylate.
6. The process for producing methyl methacrylate according to claim 5, wherein the hydroxyl group synthesis unit comprises a hydroxyl group synthesis reactor, a recycle gas compressor, a first flash tank and a first rectification column;
the bottom end of the hydroxyl synthesis reactor is provided with a feed inlet, the feed inlet of the hydroxyl synthesis reactor is respectively connected with the discharge hole of the methanol cracking unit and the discharge hole of the circulating gas compressor, and the feed inlet of the hydroxyl synthesis reactor is also used for being connected with the catalytic dry gas tank;
a discharge hole is formed in the top end of the hydroxyl synthesis reactor, the discharge hole of the hydroxyl synthesis reactor is connected with a feed hole of the first flash tank, and the discharge hole of the first flash tank is respectively connected with a feed hole of the circulating gas compressor and a feed hole of the first rectifying tower;
the discharge hole of the first rectifying tower is connected with the feed inlet of the aldol condensation unit;
the hydroxyl synthesis unit is used for synthesizing the hydroxyl groups, wherein the receiving mass ratio is 40-45%: 10% -15%: 10% -15% of the catalytic dry gas, the carbon monoxide and the hydrogen, carrying out hydroxyl synthesis reaction on the catalytic dry gas, the carbon monoxide and the hydrogen to obtain the propionaldehyde, and inputting the propionaldehyde into the aldol condensation unit, wherein the hydroxyl synthesis reaction comprises the following steps:
the hydroxyl synthesis reactor has a receiving mass ratio of 40-45%: 10% -15%: 10% -15% of the catalytic dry gas, the carbon monoxide and the hydrogen, performing hydroxyl synthesis reaction on the catalytic dry gas, the carbon monoxide and the hydrogen to obtain a first reaction product, and inputting the first reaction product into the first flash tank;
receiving the first reaction product through the first flash tank, carrying out flash evaporation on the first reaction product to obtain a first gas-phase product and a first liquid-phase product, and respectively inputting the first gas-phase product and the first liquid-phase product into the circulating gas compressor and the first rectifying tower;
compressing the first gas phase product by the recycle gas compressor, and inputting the compressed first gas phase product into the hydroxyl synthesis reactor for recycling;
and rectifying the first liquid phase product through the first rectifying tower to obtain propionaldehyde, and inputting the propionaldehyde into the aldol condensation unit.
7. The process for producing methyl methacrylate according to claim 5, wherein the aldol condensation unit comprises an aldol condensation reactor, a dehydration column and a second rectification column;
a feed inlet is formed in the top end of the aldol condensation reactor, and the feed inlet of the aldol condensation reactor is respectively connected with the discharge port of the hydroxyl synthesis unit and the formaldehyde tank;
a discharge hole is formed in the bottom end of the aldol condensation reactor, the discharge hole of the aldol condensation reactor is connected with the feed hole of the dehydration tower, and the discharge hole of the dehydration tower is connected with the feed hole of the second rectification tower;
the discharge hole of the second rectifying tower is connected with the feed inlet of the oxidative esterification unit;
the mass ratio of reception by the aldol condensation unit is 45-55%: 45% -55% of the methyl aldehyde and the propionaldehyde are subjected to aldol condensation reaction to obtain the methyl acrolein, and the methyl acrolein is input into the oxidation esterification unit, wherein the method comprises the following steps:
the mass ratio of the materials to be received by the aldol condensation reactor is 45-55%: performing aldol condensation reaction on 45-55% of the propionaldehyde and the formaldehyde to obtain a second reaction product, and inputting the second reaction product into the dehydration tower;
dehydrating the second reaction product through the dehydrating tower to obtain mixed methacrolein, and inputting the mixed methacrolein into the second rectifying tower;
and rectifying the mixed methacrolein through the second rectifying tower to obtain methacrolein, and inputting the methacrolein into the oxidative esterification unit.
8. A process for producing methyl methacrylate according to claim 5, wherein the oxidative esterification unit comprises an oxidative esterification reactor, a second flash tank, an extraction column and a third rectification column;
a feed inlet is formed in the top end of the oxidation esterification reactor, and the feed inlet of the oxidation esterification reactor is respectively connected with a discharge port of the aldol condensation unit and the reaction gas tank;
a discharge hole is formed in the bottom end of the oxidation esterification reactor, the discharge hole of the oxidation esterification reactor is connected with the feed hole of the second flash tank, the discharge hole of the second flash tank is connected with the feed hole of the extraction tower, and the discharge hole of the extraction tower is connected with the feed hole of the third rectification tower;
the mass ratio of the received water by the oxidation esterification unit is 5-15%: 30% to 40% of the methacrolein and the reaction gas, and subjecting the methacrolein and the reaction gas to an oxidative esterification reaction to obtain the methyl methacrylate, comprising:
the receiving mass ratio is 5-15% through the oxidation esterification reactor: 30% -40% of the methacrolein and the reaction gas, carrying out oxidation esterification reaction on the methacrolein and the reaction gas to obtain a third reaction product, and inputting the third reaction product into the second flash tank;
carrying out flash evaporation on the third reaction product through the second flash tank to obtain a second gas-phase product and a second liquid-phase product, emptying the second gas-phase product, and inputting the second liquid-phase product into the extraction tower;
receiving the second liquid-phase product through the extraction tower, extracting the second liquid-phase product to obtain mixed methyl methacrylate, and inputting the mixed methyl methacrylate into the third rectifying tower;
and rectifying the mixed methyl methacrylate by the third rectifying tower to obtain the methyl methacrylate.
9. The process for producing methyl methacrylate according to claim 8, wherein the second liquid-phase product comprises an organic phase and an aqueous phase;
receiving the second liquid-phase product through the extraction column, and extracting the second liquid-phase product to obtain mixed methyl methacrylate, wherein the mixed methyl methacrylate comprises:
and reversely contacting the second liquid-phase product with an extracting agent in the extraction tower through the extraction tower, so that the organic phase is separated from the water phase, and the mixed methyl methacrylate is obtained.
10. The process for producing methyl methacrylate according to claim 8, wherein the reaction temperature of the oxidative esterification reaction is 50 to 150 ℃ and the reaction pressure is 0.2 to 1.2MPa.
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