CN201999875U - 2-methylimidazole continuous synthesis and separation device - Google Patents
2-methylimidazole continuous synthesis and separation device Download PDFInfo
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- CN201999875U CN201999875U CN2011201083889U CN201120108388U CN201999875U CN 201999875 U CN201999875 U CN 201999875U CN 2011201083889 U CN2011201083889 U CN 2011201083889U CN 201120108388 U CN201120108388 U CN 201120108388U CN 201999875 U CN201999875 U CN 201999875U
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Abstract
The utility model discloses a 2-methylimidazole continuous synthesis and separation device, which solves the problems of high moisture evaporation capacity, high power consumption, high waste liquor and gas discharge capacity, serious carbonization and entrainment, high volatilization capacity of an open or cooling backflow system, low discontinuous operation efficiency and the like in the conventional process. The device is characterized in that: a crystallization kettle is additionally arranged between two reaction kettles and is integrally connected in series with the two reaction kettles; automatic cyclic liquid seal pressure control devices are arranged on front and back reaction kettles; the inlet ends of pumps of the devices are connected with a pipeline which is inserted into a middle crystallization kettle (2) through communication valves, and the outlet ends of the pumps of the devices are connected with spray nozzles arranged in absorption columns through conveying pipelines respectively; a liquid outlet at the bottom of a reaction kettle (1) is connected with a liquid inlet on the upper part of the crystallization kettle (2) through a communication valve and is connected with an evaporator (4) through a communication valve; and a liquid outlet at the bottom of a reaction kettle (3) is connected with the evaporator (4) through a pipeline and a communication valve. The device has the advantages of low carbon, environment friendliness, continuity of production and the like, and is an ideal facility for technical transformation in a 2-methylimidazole production enterprise.
Description
One, technical field
The utility model relates to the solution-air phase high density chemical reaction equipment that a kind of easy molten gas participates in, and relates in particular to the continuously synthetic isolating equipment configuration of a kind of glyoxal ethyline.
Two, background technology
Existing glyoxal ethyline production technique is:
Acetaldehyde
(aqueous solution)+ oxalic dialdehyde
(aqueous solution)+ ammoniacal liquor → glyoxal ethyline
Acetaldehyde
(aqueous solution)+ oxalic dialdehyde
(aqueous solution)+ bicarbonate of ammonia
(aqueous solution)→ glyoxal ethyline
Acetaldehyde
(aqueous solution)+ oxalic dialdehyde
(aqueous solution)+ ammonium oxalate
(aqueous solution)→ glyoxal ethyline
Above-mentioned production technique all is the homogeneous reaction production technique, will add about 60% water before all having reaction in raw material, after the reaction again evaporation remove and add and the water of reaction generation.Make that energy consumption height, waste liquid, gas quantity discharged are big, carbonization, carry secretly serious; Problem such as also exist to open wide or the volatilization of cooling for reflux system is many, periodical operation efficient is low.
Three, summary of the invention
The purpose of this utility model can significantly reduce the water evaporates amount in order to provide a kind of exactly, and the system that guarantees again is in the normal pressure sealed state, also accomplishes the device of continuous production (constantly feed intake, constantly draw product).
The technical scheme that the utility model adopted is: it is by reactor, absorption column, fractional column, condenser, pipeline, formation such as pressure inductor and liquid seal trough, at two crystallization kettles of the middle series connection of reactor that are provided with self-poking arrangement, and preceding, the top of afterreaction still is provided with automated cycle fluid-tight pressure control device, this device is by absorption column, pump, pressure inductor and liquid seal trough are formed, pressure inductor is installed on the side top of liquid seal trough, and in liquid seal trough, establish two ball floats, the entrance end of pump links to each other by the pipeline in the middle crystallization kettle of communicating valve and insertion, its exit end links to each other with shower nozzle in being arranged at absorption column by transport pipe respectively, and the absorption column top links to each other with liquid seal trough by pipeline; First reactor bottom leakage fluid dram links to each other by the fluid inlet of communicating valve with intermediate reaction still top, and links to each other with vaporizer by communicating valve; The 3rd reactor bottom leakage fluid dram links to each other with vaporizer with communicating valve by pipeline, establishes fractional column on vaporizer, and is provided with condenser on the fractional column top, and the fractional column top links to each other with the raw material gas ammonia by pipeline.Reactor bottom leakage fluid dram links to each other by the fluid inlet of communicating valve with crystallization kettle top, and links to each other with vaporizer by communicating valve; Reactor bottom leakage fluid dram links to each other with vaporizer with communicating valve by pipeline, and the vaporizer top links to each other with the raw material gas ammonia by pipeline.
The utility model compared with prior art has following advantage and beneficial effect: (1) can reduce the water evaporates amount; (2) need not evaporate, when reaction was carried out, the product that has can be separated out by direct crystallization; (3) reactive system can be controlled at the normal pressure sealed state automatically; (4) energy continuous automatic production; (5) reduce that water vapor is carried material quantity secretly, reduced heat organic carbon amount, the normal pressure tightness system is stopped the small molecules volatility of raw material; (6) can reclaim excess of ammonia gas; (7) product yield improves greatly.
Four, description of drawings
Fig. 1 is the utility model structural representation.
Among the figure: 1 is reactor, and 2 is crystallization kettle, and 3 is reactor, and 4 is vaporizer, and 5 is absorption column, and 6 is pressure inductor, and 7 is liquid seal trough, and 8 is pressure inductor, and 9 is liquid seal trough, and 10 is absorption column.
Below in conjunction with accompanying drawing the utility model is further described.
Five, embodiment
As shown in Figure 1, at two crystallization kettles of the middle series connection of reactor that are provided with self-poking arrangement, on first reactor 1, establish automated cycle fluid-tight pressure control device, this device is made up of absorption column 5, pump, pressure inductor 6 and liquid seal trough 7, pressure inductor 6 is installed on the side top of liquid seal trough 7, and in liquid seal trough 7, establish two ball floats, the entrance end of pump links to each other by the pipeline in the middle crystallization kettle 2 of communicating valve and insertion, its exit end links to each other with shower nozzle in being arranged at absorption column 5 by transport pipe, and absorption column 5 tops link to each other with liquid seal trough 7 by pipeline.The same automated cycle fluid-tight pressure control device that constitutes by absorption column 10, pump, pressure inductor 8 and liquid seal trough 9 that is provided with on the 3rd reactor 3, pressure inductor 8 is installed on the side top of liquid seal trough 9, and in liquid seal trough 9, establish two ball floats, the entrance end of pump links to each other by the pipeline in the middle crystallization kettle 2 of communicating valve and insertion, its exit end links to each other with shower nozzle in being arranged at absorption column 10 by transport pipe, and absorption column 10 tops link to each other with liquid seal trough 9 by pipeline.Reactor 1 bottom leakage fluid dram links to each other by the fluid inlet of communicating valve with crystallization kettle 2 tops, and links to each other with vaporizer 4 by communicating valve; Reactor 3 bottom leakage fluid drams link to each other with vaporizer 4 with communicating valve by pipeline, and vaporizer 4 tops link to each other with the raw material gas ammonia by pipeline.
When implementing the utility model, only need to add mother liquor control normal pressure, temperature control to reactor 1, feed pure raw material continuously, reaction solution constantly flows into crystallization kettle 2, without the evaporative crystallization still with regard to crystalline product (as: knowing that by material balance glyoxal ethyline is crystallizable separates out nearly 60%), a crystalline mother solution part refluxes through absorption column, another part is filled with reactor 3, after control normal pressure, the temperature reaction, sends to evaporating, concentrating and crystallizing.The key of this technology is by the mother liquor partial reflux, has both controlled reactor 1 reaction density at optimum range, and the system that guarantees again is in the normal pressure sealed state, also accomplishes continuous production (constantly feed intake, constantly product is separated out in crystallization).
Adopt the utility model Synthetic 2-Methylimidazole, have low-carbon (LC) (saving moisture content evaporation energy 60%), environmental protection (avoiding reactant vapor and gas loss, minimizing solvent vapo(u)r to carry secretly), efficient (energy efficient, as: glyoxal ethyline is saved water evaporates and is taken 1800 yuan/ton of 3000 * 60% ≈, by 7000 tons/yearly capacity, economic benefit increases more than 1,000 ten thousand yuan/year; Productive rate improves: glyoxal ethyline can run off (pollution) by reducing, and improves more than the productive rate 5-10%; Also have continuous production synergy) wait remarkable advantage, will bring abundant economic benefit for enterprise's production, be the optimal selection that glyoxal ethyline manufacturing enterprise undergoes technological transformation.
Claims (1)
1. continuous synthesizing and separating device of glyoxal ethyline, it comprises reactor, absorption column, fractional column, condenser, pipeline, pressure inductor and liquid seal trough, it is characterized in that: at two crystallization kettles of the middle series connection of reactor that are provided with self-poking arrangement, and preceding, the top of two reactors in back is provided with automated cycle fluid-tight pressure control device, this device is by absorption column, pump, pressure inductor and liquid seal trough are formed, pressure inductor is installed on the side top of liquid seal trough, and in liquid seal trough, establish two ball floats, the entrance end of pump links to each other by the pipeline in the middle crystallization kettle of communicating valve and insertion, its exit end links to each other with shower nozzle in being arranged at absorption column by transport pipe respectively, and the absorption column top links to each other with liquid seal trough by pipeline; Reactor (1) bottom leakage fluid dram links to each other by the fluid inlet of communicating valve with crystallization kettle (2) top, and links to each other with vaporizer (4) by communicating valve; Reactor (3) bottom leakage fluid dram links to each other with vaporizer (4) with communicating valve by pipeline, and vaporizer (4) top links to each other with the raw material gas ammonia by pipeline.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011201083889U CN201999875U (en) | 2011-04-12 | 2011-04-12 | 2-methylimidazole continuous synthesis and separation device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011201083889U CN201999875U (en) | 2011-04-12 | 2011-04-12 | 2-methylimidazole continuous synthesis and separation device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN201999875U true CN201999875U (en) | 2011-10-05 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2011201083889U Expired - Fee Related CN201999875U (en) | 2011-04-12 | 2011-04-12 | 2-methylimidazole continuous synthesis and separation device |
Country Status (1)
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| CN (1) | CN201999875U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114276299A (en) * | 2021-11-08 | 2022-04-05 | 山东友泉新材料有限公司 | Continuous preparation method of 4-methylimidazole |
-
2011
- 2011-04-12 CN CN2011201083889U patent/CN201999875U/en not_active Expired - Fee Related
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114276299A (en) * | 2021-11-08 | 2022-04-05 | 山东友泉新材料有限公司 | Continuous preparation method of 4-methylimidazole |
| CN114276299B (en) * | 2021-11-08 | 2024-04-05 | 山东友泉新材料有限公司 | Continuous preparation method of 4-methylimidazole |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C17 | Cessation of patent right | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20111005 Termination date: 20120412 |