CN215162271U - Energy-saving methyl mercaptan synthesizing device - Google Patents
Energy-saving methyl mercaptan synthesizing device Download PDFInfo
- Publication number
- CN215162271U CN215162271U CN202120813203.8U CN202120813203U CN215162271U CN 215162271 U CN215162271 U CN 215162271U CN 202120813203 U CN202120813203 U CN 202120813203U CN 215162271 U CN215162271 U CN 215162271U
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- Prior art keywords
- preheater
- gas
- reactor
- heat
- refrigerator
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- LSDPWZHWYPCBBB-UHFFFAOYSA-N Methanethiol Chemical compound SC LSDPWZHWYPCBBB-UHFFFAOYSA-N 0.000 title claims abstract description 49
- 230000002194 synthesizing effect Effects 0.000 title claims description 5
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims abstract description 66
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 22
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 21
- 239000007788 liquid Substances 0.000 claims abstract description 21
- 238000005507 spraying Methods 0.000 claims description 8
- 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
- 239000007789 gas Substances 0.000 abstract description 62
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 abstract description 11
- 229910000037 hydrogen sulfide Inorganic materials 0.000 abstract description 11
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 8
- 238000000926 separation method Methods 0.000 abstract description 7
- 239000011261 inert gas Substances 0.000 abstract description 5
- 238000010521 absorption reaction Methods 0.000 abstract description 4
- 238000005406 washing Methods 0.000 abstract description 4
- 238000005265 energy consumption Methods 0.000 abstract description 2
- 238000001816 cooling Methods 0.000 abstract 1
- 239000012071 phase Substances 0.000 description 5
- 238000009833 condensation Methods 0.000 description 4
- 230000005494 condensation Effects 0.000 description 4
- 238000000034 method Methods 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
- 239000000203 mixture Substances 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 230000009466 transformation Effects 0.000 description 3
- 238000006555 catalytic reaction Methods 0.000 description 2
- 238000001311 chemical methods and process Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 238000000844 transformation Methods 0.000 description 2
- QMMFVYPAHWMCMS-UHFFFAOYSA-N Dimethyl sulfide Chemical compound CSC QMMFVYPAHWMCMS-UHFFFAOYSA-N 0.000 description 1
- ZNZNXSDPNKCWNO-UHFFFAOYSA-N S.CO Chemical compound S.CO ZNZNXSDPNKCWNO-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
- 238000012824 chemical production Methods 0.000 description 1
- 238000010924 continuous production Methods 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 238000010586 diagram 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
- 238000010438 heat treatment Methods 0.000 description 1
- 239000000575 pesticide Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 229920002994 synthetic fiber Polymers 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
Images
Classifications
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model discloses an energy-conserving methyl mercaptan synthesizer, including blender, preheater one, preheater two, preheater three, reactor, heat taker, multistage condenser, compressor, tail gas scrubber, methyl alcohol precooler, refrigerator and vapour and liquid separator. Pre-cooling methanol, washing part of circulating gas, emptying non-condensable gas after gas-liquid separation, mixing absorption liquid with hydrogen sulfide, sequentially preheating by a first preheater, a second preheater and a third preheater, and then entering a reactor; the heat medium enters from the lower part of the reactor and is discharged after heat exchange of the first preheater; the synthesis gas produced by the reactor sequentially passes through a second preheater, a first preheater and a heat collector for heat exchange and then enters a multistage condenser for separating crude mercaptan, the uncondensed gas phase is pressurized by a compressor, then one part of the uncondensed gas phase enters a tail gas washing device, and the other part of the uncondensed gas phase and hydrogen sulfide enter a mixer together; the heat from the heat collector is made into chilled water by a refrigerator and then precooled into methanol. The device has the advantages of full heat utilization, reasonable inert gas and hydrogen sulfide separation process and obvious energy consumption reduction.
Description
Technical Field
The utility model belongs to the chemical production field especially relates to an energy-conserving methyl mercaptan synthesizer.
Background
Methyl mercaptan belongs to a mercaptan organic substance which has the smallest relative molecular mass and is very active and is easy to react with other substances to form a sulfur-containing substance, 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 and hydrogen sulfide, with significant improvements in the pretreatment of the feed gas mixture and the utilization of the heat of reaction and 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 methanol evaporation and preheating is still 100-150 ℃, the temperature is higher in actual production, 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 adopting hydrogen sulfide-methanol catalytic reaction, wherein the heat of synthesis gas is only used for methanol evaporation and preheating, the preheating of raw materials to the reaction temperature in a catalyst bed layer is difficult to realize in the actual production, 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 1189487A discloses a separation method of a product gas mixture for catalytic synthesis of methyl mercaptan, wherein a residual gas flow enters into secondary washing and distillation after product gas at 100-150 ℃ is subjected to secondary condensation. The waste heat of the synthesis gas is not fully utilized; the content of inert gas components in the mercaptan synthesis reaction is very low (less than 5%), and the total washing of the residual gas is uneconomical, since the reaction requires the amount of recycle gas to be adequate.
CN 111167267A discloses a recycle system of hydrogen sulfide in methyl mercaptan synthesis tail gas, uses methanol to absorb hydrogen sulfide in synthesis tail gas, and the residual gas is emptied after passing through a first cooler and a gas-liquid separation tank. Small liquid drops in the residual gas are removed in a condensation mode, so that the consumption of a cooling medium is increased, and the investment is increased.
Disclosure of Invention
In order to solve the problems, the utility model aims at providing an energy-saving methyl mercaptan synthesizer, the heat utilization is abundant, the inert gas is got rid of the flow rationally, and the energy consumption is showing and is reducing.
The purpose of the utility model is realized like this:
an energy-saving methyl mercaptan synthesizing device is characterized in that: comprises a mixer 1, a first preheater 2, a second preheater 3, a third preheater 4, a reactor 5, a heat collector 6, a multi-stage 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 outlet of the mixer is sequentially connected with the upper part of the reactor 5 through the tube passes of the first preheater 2, the second preheater 3 and the third preheater 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 a second preheater 3 and a first preheater 2; the first preheater 2 is sequentially connected with a heat collector 6 and a multi-stage condenser 7; the multistage condenser 7 is respectively connected with a compressor 8 and a crude mercaptan removing and separating device 13; the outlet of the compressor 8 is connected with a tail gas scrubber 9; the other side of the heat collector 6 is connected withThe refrigerator 11 is connected with the methanol precooler 10; the upper part of the tail gas scrubber 9 is connected with the shell pass of a methanol precooler 10, and the gas phase at the top part is sent to H after passing through a gas-liquid separator 122An S recovery unit or a tail gas incineration unit 14.
The further design is that: the reactor 5 is a tubular reactor.
The further design is that: the heat collector 6 is a heat exchanger commonly used in the chemical process.
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 refrigerator.
The further design is that: the tail gas scrubber 9 is provided with a self-circulation spraying pipeline, and the spraying position of the self-circulation spraying pipeline is arranged at the middle upper part.
The further design is that: the gas-liquid separator 12 is a double-baffle gas-liquid separator.
Further, the reactor is a tubular reactor;
the gas flow ratio from a compressor to a mixer and a tail gas scrubber of the device is 1-10;
compared with the prior art, the beneficial effects of the utility model reside in that:
the utility model discloses reasonable in process, inert gas and hydrogen sulfide separation flow are reasonable, do not have unnecessary process, and the heat utilization is abundant, and the cooling water consumption is low, is fit for newly-built device and current device's transformation upgrading.
Drawings
Fig. 1 is a schematic structural view of the present invention;
wherein, the method comprises the steps of 1, a mixer, 2, a first preheater, 3, a second preheater, 4, a third 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 crude mercaptan removal separation device, 14, H2S recovery or tail gas incineration device, 15, methanol, 16 and recycle gas;
FIG. 2 is a schematic diagram of a tail gas scrubber.
Detailed Description
The technical solutions in the embodiments of the present invention will be described clearly and completely with reference to the accompanying drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only some embodiments of the present invention, not all embodiments. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative work belong to the protection scope of the present 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 remover 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 outlet of the mixer is sequentially connected with the upper part of the reactor 5 through the tube passes of the first preheater 2, the second preheater 3 and the third preheater 4; the shell side of the preheater III 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 a second preheater 3 and a first preheater 2 in sequence; the first preheater 2 is sequentially connected with a heat collector 6 and a multi-stage condenser 7; the multistage condenser 7 is respectively connected with a compressor 8 and a crude mercaptan removing and separating device 13; the outlet of the compressor 8 is connected with a tail 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 pass of a methanol precooler 10, and the gas phase at the top part is sent to H after passing through a gas-liquid separator 122S recovery or tail gas incineration unit 14.
The further design is that: the heat collector 6 is a heat exchanger commonly used in the chemical process.
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 refrigerator.
The further design is that: the tail gas scrubber 9 is provided with a self-circulation spraying pipeline, and the spraying position is at the middle upper part.
Further, the reactor is a tubular reactor;
the methanol 15 is pre-cooled to-5 ℃ to 5 ℃ by a methanol pre-cooler 10 and then enters the upper part of a tail gas scrubber 9 to spray and absorb part of the recycle gas, the absorption liquid is sent to a mixer 1 to be mixed with another recycle gas 16 (containing hydrogen sulfide supplement) and then exchanges heat with the synthesis gas in a first preheater 2 to 70 ℃ to 90 ℃, exchanges heat with the synthesis gas in a second preheater 3 to 140 ℃ to 200 ℃, exchanges heat with a heating medium in a third preheater 4 to 250 ℃ to 300 ℃ and then enters a reactor 5, and the components of the synthesis gas produced by the reactor 5 are about 88% of methyl mercaptan, 9% of methyl sulfide and 3% of inert components. The temperature of the synthesis gas is about 150 ℃ after heat exchange through the first preheater 2, the second preheater 3 and the third preheater 4.
The synthesis gas with the temperature of 120-150 ℃ exchanges heat with hot water in the heat collector 6 to obtain hot water with the temperature of about 100 ℃ and the hot water enters the refrigerator 11, the chilled water produced in the refrigerator 11 supplies cold for the methanol precooler 10, and the insufficient part can be supplied by the boundary area chilled water. The synthesis gas after heat exchange enters a multistage condenser 7 for separating a gas phase and a liquid phase, the liquid phase is sent to a separation device for purifying methyl mercaptan, the gas phase is pressurized by a compressor, then a part of the gas phase is sent to a tail gas scrubber 9 for absorption, the absorbed inert gas is sent to a gas-liquid separator 12 for recycling the liquid phase and then sent to a H2S recovery unit or tail gas burning unit; the other part of the circulating gas and the supplemented hydrogen sulfide and the absorption liquid enter a mixer together to form a closed loop.
The gas-liquid separator 12 is a multi-gear gas-liquid separator, and has no public engineering consumption.
The gas flow ratio from the compressor 8 to the mixer 1 and the tail gas scrubber 9 is 1-10, usually 4.
The present invention is not limited to the above embodiments, and based on the technical solutions disclosed in the present invention, those skilled in the art can make some replacements and transformations for some technical features without creative labor according to the disclosed technical contents, and these replacements and transformations are all within the protection scope of the present invention.
Claims (6)
1. An energy-saving methyl mercaptan synthesizing device is characterized in that: comprises a mixer (1), a first preheater (2), a second preheater (3) and a third preheater (4)The system comprises a reactor (5), a heat extractor (6), a multi-stage 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 outlet of the mixer is connected with the upper part of the reactor (5) through the tube passes of the first preheater (2), the second preheater (3) and the third preheater (4) in sequence; 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 pass of a second preheater (3) and a first preheater (2); the first preheater (2) is sequentially connected with the heat collector (6) and the multistage condenser (7); the multistage condenser (7) is respectively connected with a compressor (8) and a crude mercaptan removing and separating device (13); the outlet of the compressor (8) is connected with a tail 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 H after passing through a gas-liquid separator (12)2S recovery or tail gas incineration device (14).
2. An energy-saving methyl mercaptan synthesis plant according to claim 1, wherein: the reactor (5) is a tubular reactor.
3. An energy-saving methyl mercaptan synthesis plant according to claim 1, wherein: the heat collector (6) is a shell-and-tube heat exchanger.
4. An energy-saving methyl mercaptan synthesis plant according to claim 1, wherein: the refrigerator (11) can be a lithium bromide refrigerator, an organic refrigerator or an ammonia refrigerator.
5. An energy-saving methyl mercaptan synthesis plant according to claim 1, wherein: the tail gas scrubber (9) is provided with a self-circulation spraying pipeline, and the spraying position of the self-circulation spraying pipeline is arranged at the middle upper part.
6. An energy-saving methyl mercaptan synthesis plant according to claim 1, wherein: the gas-liquid separator (12) is a double-baffle gas-liquid separator.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202120813203.8U CN215162271U (en) | 2021-04-20 | 2021-04-20 | Energy-saving methyl mercaptan synthesizing device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202120813203.8U CN215162271U (en) | 2021-04-20 | 2021-04-20 | Energy-saving methyl mercaptan synthesizing device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN215162271U true CN215162271U (en) | 2021-12-14 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202120813203.8U Withdrawn - After Issue CN215162271U (en) | 2021-04-20 | 2021-04-20 | Energy-saving methyl mercaptan synthesizing device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN215162271U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112979516A (en) * | 2021-04-20 | 2021-06-18 | 查都(海南)科技有限公司 | Energy-saving methyl mercaptan synthesizing device |
-
2021
- 2021-04-20 CN CN202120813203.8U patent/CN215162271U/en not_active Withdrawn - After Issue
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112979516A (en) * | 2021-04-20 | 2021-06-18 | 查都(海南)科技有限公司 | Energy-saving methyl mercaptan synthesizing device |
| CN112979516B (en) * | 2021-04-20 | 2023-12-08 | 查都(海南)科技有限公司 | Energy-saving methyl mercaptan synthesis device |
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| AV01 | Patent right actively abandoned |
Granted publication date: 20211214 Effective date of abandoning: 20231208 |
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| AV01 | Patent right actively abandoned |
Granted publication date: 20211214 Effective date of abandoning: 20231208 |
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