CN112979516B - Energy-saving methyl mercaptan synthesis device - Google Patents
Energy-saving methyl mercaptan synthesis device Download PDFInfo
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- CN112979516B CN112979516B CN202110427023.0A CN202110427023A CN112979516B CN 112979516 B CN112979516 B CN 112979516B CN 202110427023 A CN202110427023 A CN 202110427023A CN 112979516 B CN112979516 B CN 112979516B
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- preheater
- gas
- reactor
- heat
- methyl mercaptan
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- LSDPWZHWYPCBBB-UHFFFAOYSA-N Methanethiol Chemical compound SC LSDPWZHWYPCBBB-UHFFFAOYSA-N 0.000 title claims abstract description 51
- 238000003786 synthesis reaction Methods 0.000 title claims abstract description 24
- 230000015572 biosynthetic process Effects 0.000 title claims abstract description 23
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims abstract description 72
- 239000007788 liquid Substances 0.000 claims abstract description 20
- 238000000926 separation method Methods 0.000 claims abstract description 10
- 239000007921 spray Substances 0.000 claims description 9
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 6
- AMXOYNBUYSYVKV-UHFFFAOYSA-M lithium bromide Chemical compound [Li+].[Br-] AMXOYNBUYSYVKV-UHFFFAOYSA-M 0.000 claims description 6
- 238000011084 recovery Methods 0.000 claims description 5
- 229910021529 ammonia Inorganic materials 0.000 claims description 3
- 230000002194 synthesizing effect Effects 0.000 claims description 3
- 239000007789 gas Substances 0.000 abstract description 55
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 abstract description 16
- 229910000037 hydrogen sulfide Inorganic materials 0.000 abstract description 15
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 7
- 239000011261 inert gas Substances 0.000 abstract description 5
- 238000010521 absorption reaction Methods 0.000 abstract description 3
- 238000005265 energy consumption Methods 0.000 abstract description 2
- 238000010438 heat treatment Methods 0.000 abstract description 2
- 238000005406 washing Methods 0.000 abstract description 2
- 238000009833 condensation Methods 0.000 description 4
- 230000005494 condensation Effects 0.000 description 4
- 239000012071 phase Substances 0.000 description 4
- 238000006243 chemical reaction Methods 0.000 description 3
- 239000000498 cooling water Substances 0.000 description 3
- 238000001704 evaporation Methods 0.000 description 3
- 230000008020 evaporation Effects 0.000 description 3
- 239000007791 liquid phase Substances 0.000 description 3
- 238000000034 method Methods 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 238000006555 catalytic reaction Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 238000006467 substitution reaction Methods 0.000 description 2
- QMMFVYPAHWMCMS-UHFFFAOYSA-N Dimethyl sulfide Chemical compound CSC QMMFVYPAHWMCMS-UHFFFAOYSA-N 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 238000007036 catalytic synthesis reaction Methods 0.000 description 1
- 238000001311 chemical methods and process Methods 0.000 description 1
- 238000012824 chemical production Methods 0.000 description 1
- 238000010924 continuous production Methods 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 229940079593 drug Drugs 0.000 description 1
- 235000013305 food Nutrition 0.000 description 1
- 239000000575 pesticide Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 229920002994 synthetic fiber Polymers 0.000 description 1
- 150000003573 thiols Chemical class 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C319/00—Preparation of thiols, sulfides, hydropolysulfides or polysulfides
- C07C319/02—Preparation of thiols, sulfides, hydropolysulfides or polysulfides of thiols
- C07C319/08—Preparation of thiols, sulfides, hydropolysulfides or polysulfides of thiols by replacement of hydroxy groups or etherified or esterified hydroxy groups
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/24—Stationary reactors without moving elements inside
- B01J19/2415—Tubular reactors
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/06—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds in tube reactors; the solid particles being arranged in tubes
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C319/00—Preparation of thiols, sulfides, hydropolysulfides or polysulfides
- C07C319/26—Separation; Purification; Stabilisation; Use of additives
- C07C319/28—Separation; Purification
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
- F25B15/00—Sorption machines, plants or systems, operating continuously, e.g. absorption type
- F25B15/02—Sorption machines, plants or systems, operating continuously, e.g. absorption type without inert gas
- F25B15/06—Sorption machines, plants or systems, operating continuously, e.g. absorption type without inert gas the refrigerant being water vapour evaporated from a salt solution, e.g. lithium bromide
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D7/00—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Abstract
The invention discloses an energy-saving methyl mercaptan synthesis device which comprises a mixer, a first preheater, a second preheater, a third preheater, a reactor, a heat collector, a multistage condenser, a compressor, a tail gas scrubber, a methanol precooler, a refrigerator and a gas-liquid separator. The methanol is pre-cooled and then is washed with part of circulating gas, noncondensable gas is discharged after gas-liquid separation, and absorption liquid and hydrogen sulfide are mixed and then enter a reactor after being preheated by a first preheater, a second preheater and a third preheater in sequence; the heating medium enters from the lower part of the reactor and is discharged after heat exchange by the preheater I; the synthesis gas produced by the reactor sequentially passes through a preheater II, a preheater I and a heat collector to exchange heat and then enters a multistage condenser to separate crude mercaptan, a part of the non-condensable gas phase is pressurized by a compressor and then enters a tail gas washing device, and the other part of the non-condensable gas phase enters a mixer together with hydrogen sulfide; the heat extracted by the heat extractor is precooled by methanol after refrigerating water by a refrigerating machine. The device has the advantages of full heat utilization, reasonable separation flow of inert gas and hydrogen sulfide, and obviously reduced energy consumption.
Description
Technical Field
The invention belongs to the field of chemical production, and particularly relates to an energy-saving methyl mercaptan synthesis device.
Background
Methyl mercaptan belongs to thiol organic matters with the minimum relative molecular mass, is very active and is easy to react with other matters to form sulfur-containing matters, so that the methyl mercaptan has wide application and is a main raw material for synthesizing pesticides, medicines, foods, synthetic materials and the like.
CN 1186067a discloses a process for the continuous production of methyl mercaptan by catalytic reaction of methanol with hydrogen sulphide, the significant improvements being the pretreatment of the feed gas mixture and the heat of reaction and the use of heat in the product gas mixture. The heat of the synthesis gas is only used for methanol evaporation and preheating, the temperature of the synthesis gas after the methanol evaporation and preheating is still 100-150 ℃, and the temperature is higher in actual production, so that the heat of the synthesis gas is taken away by cooling water of multi-stage condensation, and the heat and circulating water are wasted.
CN 202415415U discloses a device for preparing methyl mercaptan by catalytic reaction of hydrogen sulfide and methanol, wherein the heat of synthesis gas is only used for methanol evaporation and preheating, preheating raw materials to reaction temperature in a catalyst bed is difficult to realize in actual production, and the heat of synthesis gas is taken away by cooling water of multistage condensation, so that heat is wasted and circulating water is wasted.
CN 1189487a discloses a separation method for catalytic synthesis of methyl mercaptan product gas mixture, after secondary condensation of 100-150 ℃ product gas, the residual gas flow enters into secondary washing and distillation. The waste heat of the synthesis gas is not fully utilized; the inert gas component content in the mercaptan synthesis reaction is very low (less than 5%), and it is uneconomical to completely scrub the residual gas because the reaction requires a recycle gas amount to achieve a proper molar ratio.
CN 111167267a discloses a recycling system of hydrogen sulfide in methyl mercaptan synthesis tail gas, methanol is used to absorb hydrogen sulfide in the synthesis tail gas, and residual gas is vented after passing through a first cooler and a gas-liquid separation tank. The droplets in the residual gas are removed by condensation, which increases both the consumption of the cooling medium and the investment.
Disclosure of Invention
In order to solve the problems, the invention aims to provide an energy-saving methyl mercaptan synthesis device which has the advantages of full heat utilization, reasonable inert gas removal flow and obviously reduced energy consumption.
The purpose of the invention is realized in the following way:
an energy-saving methyl mercaptan synthesizing device is characterized in that: the device comprises a mixer 1, a first preheater 2, a second preheater 3, a third preheater 4, a reactor 5, a heat collector 6, a multistage condenser 7, a compressor 8, a tail gas scrubber 9, a methanol precooler 10, a refrigerator 11 and a gas-liquid separator 12; the inlet of the mixer 1 is respectively connected with the bottom of the tail gas scrubber 9 and the outlet of the compressor 8, and the outlets of the mixer are connected with the upper part of the reactor 5 through the tube passes of the preheater I2, the preheater II 3 and the preheater III 4 in sequence; the shell side of the third preheater 4 is connected with the upper part of the shell side of the reactor 5; the lower part of the reactor 5 sequentially passes through the shell passes of the preheater II 3 and the preheater I2; the first preheater 2 is sequentially connected with the heat collector 6 and the multistage condenser 7; the lower part of the multistage condenser 7 is connected with the compressor 8, and the bottom is connected with the methyl mercaptan separation device 13; the outlet of the compressor 8 is connected with an exhaust gas scrubber 9; the other side of the heat collector 6 is connected with a refrigerator 11 and a methanol precooler 10 in sequence; the upper part of the tail gas scrubber 9 is connected with the shell side of the methanol precooler 10, and the top gas phase is sent to an H2S recovery device or a tail gas incineration device 14 after passing through a gas-liquid separator 12.
The further design is that: the reactor 5 is a tubular reactor.
The further design is that: the heat collector 6 is a shell-and-tube heat exchanger.
The further design is that: the refrigerator 11 may be a lithium bromide refrigerator, an organic refrigerator or an ammonia cooler.
The further design is that: the tail gas scrubber 9 is provided with a self-circulation spray pipeline, and the spray position of the self-circulation spray pipeline is in the middle upper part.
The further design is that: the gas-liquid separator 12 is a double-baffle gas-liquid separator.
Compared with the prior art, the invention has the beneficial effects that:
the invention has reasonable process, reasonable separation flow of inert gas and hydrogen sulfide, no redundant working procedures, full heat utilization and low cooling water consumption, and is suitable for reconstruction and upgrading of newly-built devices and existing devices.
Drawings
FIG. 1 is a schematic diagram of the structure of the present invention;
the device comprises a mixer 1, a mixer 2, a preheater I, a preheater II, a preheater 4, a preheater III, a preheater 5, a reactor 6, a heat collector 7, a multistage condenser 8, a compressor 9, a tail gas scrubber 10, a methanol precooler 11, a refrigerator 12, a gas-liquid separator 13, a methyl mercaptan separation device 14, a H2S recovery or tail gas incineration device 15, a methanol tank 16 and a hydrogen sulfide compressor;
fig. 2 is a schematic diagram of the exhaust scrubber structure.
Detailed Description
The following description of the embodiments of the present invention will be made clearly and completely with reference to the accompanying drawings, in which it is apparent that the embodiments described are only some embodiments of the present invention, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.
An energy-saving methyl mercaptan synthesis device comprises a mixer 1, a first preheater 2, a second preheater 3, a third preheater 4, a reactor 5, a heat collector 6, a multistage condenser 7, a compressor 8, a tail gas scrubber 9, a methanol precooler 10, a refrigerator 11 and a gas-liquid separator 12; the inlet of the mixer 1 is respectively connected with the bottom of the tail gas scrubber 9 and the outlet of the compressor 8, and the outlets of the mixer are connected with the upper part of the reactor 5 through the tube passes of the preheater I2, the preheater II 3 and the preheater III 4 in sequence; the shell side of the third preheater 4 is connected with the upper part of the shell side of the reactor 5; the reactor 5 is a tubular reactor, and the lower part of the reactor passes through the shell pass of the preheater II 3 and the preheater I2 in sequence; the first preheater 2 is sequentially connected with the heat collector 6 and the multistage condenser 7; the lower part of the multistage condenser 7 is connected with the compressor 8, and the bottom is connected with the methyl mercaptan separation device 13; the outlet of the compressor 8 is connected with an exhaust gas scrubber 9; the other side of the heat collector 6 is connected with a refrigerator 11 and a methanol precooler 10 in sequence; the upper part of the tail gas scrubber 9 is connected with the shell side of the methanol precooler 10, and the top gas phase is sent to the H2S recovery or tail gas incineration device 14 after passing through the gas-liquid separator 12.
The further design is that: the heat collector 6 is a heat exchanger commonly used in chemical processes.
The further design is that: the heat collector 6 is a shell-and-tube heat exchanger.
The further design is that: the refrigerator 11 may be a lithium bromide refrigerator, an organic refrigerator or an ammonia cooler.
The further design is that: the tail gas scrubber 9 is provided with a self-circulation spray pipeline, and the spray position is at the middle upper part.
Further, the reactor is a tubular reactor;
the methanol in the methanol tank 15 is pre-cooled to-5 ℃ to 5 ℃ by the methanol pre-cooler 10, then enters the upper part of the tail gas scrubber 9 to spray and absorb part of the circulating gas, the absorbing liquid is sent to the mixer 1 to be mixed with another circulating gas (containing hydrogen sulfide from the hydrogen sulfide compressor 16), then exchanges heat with the synthetic gas to 70 ℃ to 90 ℃ in the first preheater 2, exchanges heat with the synthetic gas to 140 ℃ to 200 ℃ in the second preheater 3, exchanges heat with the heating medium to 250 ℃ to 300 ℃ in the third preheater 4, and then enters the reactor 5, and the synthetic gas produced by the reactor 5 contains methyl mercaptan, methyl sulfide of 9% and inert components of 3%. The temperature of the synthesis gas after heat exchange of the first preheater 2, the second preheater 3 and the third preheater 4 is about 150 ℃.
The synthesis gas with the temperature of 120-150 ℃ exchanges heat with hot water in the heat collector 6, the hot water with the temperature of 100 ℃ is obtained and enters the refrigerator 11, chilled water produced in the refrigerator 11 is used for cooling the methanol precooler 10, and the shortage can be supplied by the boundary chilled water. The synthesis gas subjected to heat exchange is fed into a multi-stage condenser 7 for separating a gas phase and a liquid phase, the liquid phase is fed into a separation device for purifying methyl mercaptan, a part of the gas phase is fed into a tail gas scrubber 9 for absorption after being pressurized by a compressor, and the absorbed inert gas is fed into an H2S recovery device or a tail gas incineration device after the liquid phase is recovered by a gas-liquid separator 12; the other part of circulating gas, the supplementary hydrogen sulfide and the absorption liquid enter a mixer together to form a closed loop.
The gas-liquid separator 12 is a multi-stage gas-liquid separator, and has no public engineering consumption.
The ratio of the amount of air from the compressor 8 to the mixer 1 and the off-gas scrubber 9 is 1 to 10, usually 4.
The invention is not limited to the above embodiments, and based on the technical solution disclosed in the invention, a person skilled in the art may make some substitutions and modifications to some technical features thereof without creative effort according to the technical content disclosed, and all the substitutions and modifications are within the protection scope of the invention.
Claims (6)
1. An energy-saving methyl mercaptan synthesizing device is characterized in that: the device comprises a mixer (1), a first preheater (2), a second preheater (3), a third preheater (4), a reactor (5), a heat collector (6), a multistage condenser (7), a compressor (8), a tail gas scrubber (9), a methanol precooler (10), a refrigerator (11) and a gas-liquid separator (12); the inlet of the mixer (1) is respectively connected with the bottom of the tail gas scrubber (9) and the outlet of the compressor (8), and the outlets of the mixer are sequentially connected with the upper part of the reactor (5) through the tube passes of the preheater I (2), the preheater II (3) and the preheater III (4); the shell side of the preheater III (4) is connected with the upper part of the shell side of the reactor (5); the lower part of the reactor (5) sequentially passes through the shell passes of the preheater II (3) and the preheater I (2); the first preheater (2) is sequentially connected with the heat collector (6) and the multistage condenser (7); the lower part of the multistage condenser (7) is connected with the compressor (8), and the bottom is connected with the crude mercaptan separation device (13); the outlet of the compressor (8) is connected with the tail gas scrubber (9); the other side of the heat collector (6) is sequentially connected with a refrigerator (11) and a methanol precooler (10); the upper part of the tail gas scrubber (9) is connected with the shell side of the methanol precooler (10), and the top gas phase is sent to H after passing through the gas-liquid separator (12) 2 S recovery or tail gas incineration device (14).
2. An energy-efficient methyl mercaptan synthesis apparatus according to claim 1, wherein: the reactor (5) is a tubular reactor.
3. An energy-efficient methyl mercaptan synthesis apparatus according to claim 1, wherein: the heat collector (6) is a shell-and-tube heat exchanger.
4. An energy-efficient methyl mercaptan synthesis apparatus according to claim 1, wherein: the refrigerator (11) may be a lithium bromide refrigerator, an organic refrigerator or an ammonia cooler.
5. An energy-efficient methyl mercaptan synthesis apparatus according to claim 1, wherein: the tail gas scrubber (9) is provided with a self-circulation spray pipeline, and the spray position of the self-circulation spray pipeline is at the middle upper part.
6. An energy-efficient methyl mercaptan synthesis apparatus according to claim 1, wherein: the gas-liquid separator (12) is a multi-stage gas-liquid separator.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
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| CN202110427023.0A CN112979516B (en) | 2021-04-20 | 2021-04-20 | Energy-saving methyl mercaptan synthesis device |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110427023.0A CN112979516B (en) | 2021-04-20 | 2021-04-20 | Energy-saving methyl mercaptan synthesis device |
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| Publication Number | Publication Date |
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| CN112979516A CN112979516A (en) | 2021-06-18 |
| CN112979516B true CN112979516B (en) | 2023-12-08 |
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| CN113623895B (en) * | 2021-07-01 | 2022-11-01 | 华电电力科学研究院有限公司 | Combined cooling heating and power system for cooling data center and control method thereof |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1186067A (en) * | 1996-12-27 | 1998-07-01 | 底古萨股份公司 | Process for continuous production of methyl mercaptan |
| CN1189487A (en) * | 1996-12-27 | 1998-08-05 | 底古萨股份公司 | Process for separating product gas mixture from catalytic synthesis of methyl mercaptan |
| US5847223A (en) * | 1995-06-23 | 1998-12-08 | Rhone-Poulenc Nutrition Animale | Process for the preparation of methyl mercaptan |
| CN202415415U (en) * | 2011-12-21 | 2012-09-05 | 天津市泰旭物流有限公司 | Device for preparing methanethiol by use of hydrogen sulfide-methanol gas-phase catalytic reaction method |
| CN107501049A (en) * | 2017-09-19 | 2017-12-22 | 天津大学 | A kind of extracting rectifying removing low-temp methanol washes the device and method of sulfide in recycle methanol |
| CN215162271U (en) * | 2021-04-20 | 2021-12-14 | 查都(海南)科技有限公司 | Energy-saving methyl mercaptan synthesizing device |
-
2021
- 2021-04-20 CN CN202110427023.0A patent/CN112979516B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5847223A (en) * | 1995-06-23 | 1998-12-08 | Rhone-Poulenc Nutrition Animale | Process for the preparation of methyl mercaptan |
| CN1186067A (en) * | 1996-12-27 | 1998-07-01 | 底古萨股份公司 | Process for continuous production of methyl mercaptan |
| CN1189487A (en) * | 1996-12-27 | 1998-08-05 | 底古萨股份公司 | Process for separating product gas mixture from catalytic synthesis of methyl mercaptan |
| CN202415415U (en) * | 2011-12-21 | 2012-09-05 | 天津市泰旭物流有限公司 | Device for preparing methanethiol by use of hydrogen sulfide-methanol gas-phase catalytic reaction method |
| CN107501049A (en) * | 2017-09-19 | 2017-12-22 | 天津大学 | A kind of extracting rectifying removing low-temp methanol washes the device and method of sulfide in recycle methanol |
| CN215162271U (en) * | 2021-04-20 | 2021-12-14 | 查都(海南)科技有限公司 | Energy-saving methyl mercaptan synthesizing device |
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