CN218924650U - System for reducing chloromethane synthesis crude product - Google Patents
System for reducing chloromethane synthesis crude product Download PDFInfo
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- CN218924650U CN218924650U CN202223329761.0U CN202223329761U CN218924650U CN 218924650 U CN218924650 U CN 218924650U CN 202223329761 U CN202223329761 U CN 202223329761U CN 218924650 U CN218924650 U CN 218924650U
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Abstract
The utility model discloses a system for reducing the synthesis of crude products by chloromethane, which comprises a first-stage reactor, a second-stage reactor and an acid washing tower, wherein the first-stage reactor is provided with an HCL inlet and a methanol inlet, and the HCL inlet and the methanol inlet are respectively communicated with HCL and methanol; the primary reactor is provided with a primary reactor chloromethane outlet, the secondary reactor is provided with a secondary reactor chloromethane inlet, the primary reactor chloromethane outlet is communicated with the secondary reactor chloromethane inlet, the secondary reactor is provided with a secondary reactor chloromethane outlet, the pickling tower is provided with a pickling tower inlet, and the secondary reactor chloromethane outlet is communicated with the pickling tower inlet; the secondary reactor is provided with a jacket heater, and the jacket heater is provided with a steam inlet and a circulating water inlet which are respectively used for introducing steam and circulating water. The utility model reduces HCL, dimethyl ether and methanol in the chloromethane synthesized crude product and reduces the acid concentration in the subsequent acid washing process.
Description
Technical Field
The utility model relates to the field of organosilicon chloromethane reaction, in particular to a system for reducing chloromethane synthesis crude products.
Background
The disclosure of this background section is only intended to increase the understanding of the general background of the utility model and is not necessarily to be construed as an admission or any form of suggestion that this information forms the prior art already known to those of ordinary skill in the art.
At present, most of processes in the synthesis of methyl chloride in the organosilicon industry are that HCL from an analysis section is subjected to pressure stabilization treatment by a hydrogen chloride buffer tank and then is mixed and contacted with high-temperature methanol from a methanol vaporizer, and the reaction is fully contacted with zinc chloride (catalyst) in a reaction kettle through a methyl chloride reaction kettle distributor, wherein the reaction is exothermic. Wherein the main reaction equation is as follows:
CH3OH+HCl=CH3Cl+H2O+Q (143～149℃)
the side reaction equation is:
CH3OH+HOCH3=CH3OCH3+H2O (140℃)
CH3OCH3+HCl=CH3OH+CH3CL （＞100℃）
CH3OCH3+2HCl=2CH3CL+H2O
the methyl chloride gas and the water vapor are generated through the reaction, and the methyl chloride gas contains methanol, HCL and side reaction dimethyl ether which are not completely reacted.
In the operation process of the methyl chloride synthesis technology of the organic silicon device, the methyl chloride with the temperature below 45 ℃ after the crude methyl chloride is condensed also contains HCL, methanol and dimethyl ether and has partial vapor. The crude chloromethane enters the tower body at the lower part of the water washing tower, contacts with circulating primary water at the packing layer, and most of HCL gas is absorbed by the primary water and emits a large amount of heat. The reaction can bring a large amount of acid into a water scrubber system, and a large amount of waste hydrochloric acid containing 16% -27% alcohol is washed out by water in the system after the reaction. The energy consumption for treating the waste acid is high, and the cost is high.
Disclosure of Invention
In order to solve the technical problems in the prior art, the utility model provides a system for reducing the crude product of methyl chloride, reducing HCL, dimethyl ether and methanol in the crude product of methyl chloride synthesis and reducing the acid concentration in the subsequent acid washing process.
In order to solve the technical problems, the technical scheme adopted by the utility model is that the system for reducing the crude product synthesized by chloromethane comprises a first-stage reactor, a second-stage reactor and an acid washing tower, wherein the first-stage reactor is provided with an HCL-first-stage reactor inlet and a methanol-first-stage reactor inlet, the HCL-first-stage reactor inlet and the methanol-first-stage reactor inlet are respectively introduced with HCL and methanol, and the ratio of the introduced HCL and methanol is more than 1; the primary reactor is provided with a primary reactor chloromethane outlet, the secondary reactor is provided with a secondary reactor chloromethane inlet, the primary reactor chloromethane outlet is communicated with the secondary reactor chloromethane inlet, the secondary reactor is provided with a secondary reactor chloromethane outlet, the pickling tower is provided with a pickling tower inlet, and the secondary reactor chloromethane outlet is communicated with the pickling tower inlet; the secondary reactor is provided with a jacket heater, and the jacket heater is provided with a steam inlet and a circulating water inlet which are respectively used for introducing steam and circulating water.
Further, the secondary reactor chloromethane inlet is arranged at the top of the secondary reactor, and the feeding pipe of the secondary reactor chloromethane inlet penetrates into the position below the liquid level of the secondary reactor.
Further, the steam inlet of the jacket heater was fed with 1.0Mpa steam.
Further, the temperature of the secondary reactor is between 125 ℃ and 150 ℃.
Further, the secondary reactor liquid level is between 35% and 55% of its volume.
Furthermore, the acid washing tower is provided with a steam inlet, steam for stripping methanol in the crude chloromethane is introduced into the steam inlet, the stripped methanol is condensed outside the acid washing tower and used as reflux liquid of the acid washing tower, and the residual wastewater enters the next working procedure.
The utility model has the beneficial effects that: the utility model is provided with the two-stage reactors, the one-stage reactor is filled with HCL and methanol for reaction, because the ratio of HCL to methanol is more than 1, methanol can be used up as much as possible, the production of dimethyl ether in side reaction is reduced, methanol in a crude product is reduced, the rest HCL enters the two-stage reactor for continuous reaction, thereby exhausting HCL in the crude product, acidic substances in the crude product are greatly reduced after the HCL passes through the two-stage reactor, the acid concentration in the subsequent acid washing process can be reduced, methanol stripping is carried out in the acid washing tower, the methanol content in waste water after the stripping is extremely small, 0.5% of waste acid water is easy to treat, and the problems of high energy consumption and high cost of waste acid treatment are greatly solved.
Drawings
FIG. 1 is a schematic illustration of the present utility model;
in the figure: 1. HCL to the inlet of the first-stage reactor, 2 and methanol to the inlet of the first-stage reactor, 3 and the first-stage reactor, 4 and the outlet of the first-stage reactor chloromethane, 5 and the inlet of the second-stage reactor chloromethane, 6 and the second-stage reactor, 7 and the outlet of the second-stage reactor chloromethane, 8 and a jacket heater, 9 and a steam inlet, 10 and a circulating water inlet, 11 and an inlet of the pickling tower, 12 and the pickling tower.
Detailed Description
The utility model will be further described with reference to the accompanying drawings and specific examples.
Example 1
The embodiment discloses a method for reducing the synthesis of crude products by chloromethane, which comprises a primary reactor 3, a secondary reactor 6 and an acid washing tower 12, wherein the primary reactor 3 is provided with an HCL-primary reactor inlet 1, a methanol-primary reactor inlet 2, the HCL-primary reactor inlet 1, the methanol-primary reactor inlet 2 are respectively introduced with HCL and methanol, and the ratio of the introduced HCL to the methanol is more than 1, and can be specifically set to be 1.123:1.
The primary reactor 3 is provided with a primary reactor chloromethane outlet 4, the secondary reactor 6 is provided with a secondary reactor chloromethane inlet 5, the primary reactor chloromethane outlet 4 is communicated with the secondary reactor chloromethane inlet 5, the secondary reactor 6 is provided with a secondary reactor chloromethane outlet 7, the pickling tower 12 is provided with a pickling tower inlet 11, and the secondary reactor chloromethane outlet 7 is communicated with the pickling tower inlet 11. The secondary reactor 6 is externally provided with a jacket heater 8, and the jacket heater 8 is provided with a steam inlet 9 and a circulating water inlet 10 for introducing steam and circulating water respectively. And the acid washing tower is provided with a steam inlet, steam for stripping methanol in the crude chloromethane is introduced into the steam inlet, the stripped methanol is condensed outside the acid washing tower and used as reflux liquid of the acid washing tower, and the residual wastewater enters the next working procedure.
In this embodiment, the secondary reactor methyl chloride inlet 5 is disposed at the top of the secondary reactor 6, and the feed pipe of the secondary reactor methyl chloride inlet 5 goes deep below the liquid level of the secondary reactor 6. Ensures that the residual HCL and methanol raw materials fully react, prevents gas cross, and achieves the aim of reducing the direct entering of HCL into a post-purification acid washing system.
In this embodiment, the steam inlet 9 of the jacket heater 8 is fed with steam of 1.0 Mpa. The temperature and the liquid level of the secondary reactor 6 are controlled by steam (the steam is heated to adjust the temperature, and the liquid in the secondary reactor is vaporized by the temperature rise at the same time, so that the liquid level is adjusted), and the normal reaction of HCL and methanol in the secondary reactor is ensured. In the embodiment, the circulating water inlet of the jacket heater 8 is connected with a circulating water pipeline, thereby ensuring the constant control of the temperature of the secondary reactor
In this example, the secondary reactor temperature was between 125℃and 150 ℃. The secondary reactor liquid level is between 35% and 55% of its volume.
The embodiment is provided with two stages of reactors, one stage of reactor is filled with HCL and methanol for reaction, because the ratio of HCL to methanol is greater than 1, methanol can be exhausted as much as possible, the production of dimethyl ether by side reaction is reduced, methanol in a crude product is reduced, the rest HCL enters the two stages of reactors for continuous reaction, thereby exhausting HCL in the crude product, acidic substances in the crude product are greatly reduced after the HCL passes through the two stages of reactors, the acid concentration in a subsequent pickling process can be reduced, methanol stripping is carried out in a pickling tower, the methanol content in waste water after stripping is extremely small, 0.5% of waste acid water is easy to treat, and the problems of high energy consumption and high cost of waste acid treatment are greatly solved.
The acid-containing crude chloromethane generated by the reaction in the first-stage reactor enters a newly added second-stage reactor to continue the reaction, and is heated by a jacket heater of the second-stage reactor to reach the process operation temperature condition, so that 5% of HCL and 10% of methanol of the residual materials are consumed, and the purpose of reducing the synthesis of crude products of chloromethane is achieved.
While the foregoing description of the embodiments of the present utility model has been presented in conjunction with the drawings, it should be understood that the utility model is not limited to the particular embodiments, but is capable of numerous modifications and variations within the spirit and scope of the utility model.
Claims (6)
1. A system for reducing the synthesis of crude methyl chloride, comprising: the method comprises a first-stage reactor, a second-stage reactor and an acid washing tower, wherein the first-stage reactor is provided with an inlet from HCL to the first-stage reactor and an inlet from methanol to the first-stage reactor, the inlet from HCL to the first-stage reactor and the inlet from methanol to the first-stage reactor are respectively introduced with HCL and methanol, and the ratio of the introduced HCL to the methanol is more than 1; the primary reactor is provided with a primary reactor chloromethane outlet, the secondary reactor is provided with a secondary reactor chloromethane inlet, the primary reactor chloromethane outlet is communicated with the secondary reactor chloromethane inlet, the secondary reactor is provided with a secondary reactor chloromethane outlet, the pickling tower is provided with a pickling tower inlet, and the secondary reactor chloromethane outlet is communicated with the pickling tower inlet; the secondary reactor is provided with a jacket heater, and the jacket heater is provided with a steam inlet and a circulating water inlet which are respectively used for introducing steam and circulating water.
2. The system for reducing a crude product of chloromethane synthesis according to claim 1, wherein: the second-stage reactor chloromethane inlet is arranged at the top of the second-stage reactor, and the feeding pipe of the second-stage reactor chloromethane inlet penetrates into the position below the liquid level of the second-stage reactor.
3. The system for reducing a crude product of chloromethane synthesis according to claim 1, wherein: the steam inlet of the jacket heater was fed with 1.0Mpa steam.
4. The system for reducing a crude product of chloromethane synthesis according to claim 1, wherein: the temperature of the secondary reactor is between 125 ℃ and 150 ℃.
5. The system for reducing a crude product of chloromethane synthesis according to claim 1, wherein: the secondary reactor liquid level is between 35% and 55% of its volume.
6. The system for reducing a crude product of chloromethane synthesis according to claim 1, wherein: the pickling tower is provided with a steam inlet, and steam for stripping methanol in the crude chloromethane is introduced into the steam inlet.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202223329761.0U CN218924650U (en) | 2022-12-13 | 2022-12-13 | System for reducing chloromethane synthesis crude product |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202223329761.0U CN218924650U (en) | 2022-12-13 | 2022-12-13 | System for reducing chloromethane synthesis crude product |
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| Publication Number | Publication Date |
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| CN218924650U true CN218924650U (en) | 2023-04-28 |
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| CN202223329761.0U Active CN218924650U (en) | 2022-12-13 | 2022-12-13 | System for reducing chloromethane synthesis crude product |
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