CN101691333A - Production technology for choline chloride - Google Patents
Production technology for choline chloride Download PDFInfo
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- CN101691333A CN101691333A CN200910229233A CN200910229233A CN101691333A CN 101691333 A CN101691333 A CN 101691333A CN 200910229233 A CN200910229233 A CN 200910229233A CN 200910229233 A CN200910229233 A CN 200910229233A CN 101691333 A CN101691333 A CN 101691333A
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- trimethylamine
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- choline chloride
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- oxyethane
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Abstract
The invention discloses production technology for choline chloride. The technology adopts a storage tank with a magnetic flap level gage, a clean type closed anti-volatility unloading device, a gas recovery device, a matched metering system device, an one-step reaction synthesis tank suitable for the choline chloride, and a concentration device, which meets the requirements of mass production, greatly improves the productivity, reduces the discharge of three wastes, reduces energy consumption, and ensures the quality of products.
Description
Technical field
The present invention relates to a kind of production technology for choline chloride.
Background technology
Choline chloride 60, English name: choline chloride, chemical name: 2-hydroxyethyl trimethyl ammonium chloride, chemical formula: C
5H
14NOCl, molecular weight is: 139.63, it is a white crystal, has strong water absorbability.Have the salty bitter taste of fishy smell and tool slightly.Soluble in water and pure, it is neutral that the aqueous solution almost is, and is insoluble to ether, sherwood oil, benzene and dithiocarbonic anhydride, unstable in basic solution.240 ℃ of fusing points.The choline chloride aqueous solution agent storage temperature should not be lower than-12 ℃.
Choline is a kind of water-soluble vitamins VB4, is present in the fodder additives with the form of choline chloride 60.Since eighties of last century the '30s, people progressively have been familiar with its nutrition importance and all physiological functions.Choline chloride 60 has not only become the mode of direct, the most most economical additional choline of generally acknowledging, becomes the modern intensive animal and produces requisite additive, and be addition maximum today, is used for the highest vitamins product of animal ratio.Choline had become the focus that people pay close attention to again in recent years.Choline research aspect brain development and exploitation cognition, memory and learning capacity, in disease preventing and treating such as cardiovascular disorder, cancer, dementia, research as aspects such as Alzheimer (Alzheimer) diseases, promoting levels of acetylcholine, increase people's somatotropin (HGH) release, reduce tethelin and discharge the research of the factor (somatostatin) of drawing up and it and preventing and treating chronic disease and to the research aspect the elder's health effect etc.Choline aspect animal and the feed mainly is being the effect that improves the animal immune aspect, as with the conversion of immunoreactive cell, thymocyte formation, scavenger cell taxis, the lymphocytic relation of T-etc., and on the problem that the science such as optimum addition of the biological effectiveness of choline chloride 60 quality examination, natural choline and different animals, different ages are used.
The chemical synthesis process of choline chloride 60 has chloroethanol method and epoxyethane method.The chloroethanol method is that Trimethylamine 99, chloroethene alcohol and water are added in the batch operation reactor according to a certain percentage, reacting by heating, and after reaction finished, decompression removed and anhydrates, and obtains white crystals, obtains choline chloride 60 needle crystal behind the recrystallization.Epoxyethane method is with Trimethylamine 99 and hydrochloric acid reaction, generates trimethylamine hydrochloride, adds oxyethane then, and reaction back removal of impurities finally generates choline chloride 60.Chloroethanol method production technique is more convenient, but production cost is higher.Epoxyethane method technology is fairly simple, but condition is relatively harsher.Inflammable, explosive chemicals that oxyethane belongs to has proposed higher requirement to operation, transportation and deposit, and epoxyethane method requires equipment acidproof, corrosion-resistant simultaneously, but the ethylene oxide production cost is low than the chloroethanol method, is the method for generally using at present.
Summary of the invention
In order to overcome the shortcoming in the existing choline chloride 60 production, the object of the present invention is to provide a kind of synthesizing chlorinated choline of epoxyethane method that utilizes, after being concentrated into finite concentration, concentrating unit uses decolorizing with activated carbon, after flame filter press filter, obtain the production technique of required choline chloride 60 product, this production technology advanced person, constant product quality.
Technical scheme of the present invention is: a kind of production technique of choline chloride 60 may further comprise the steps: (1) utilizes the raw material unloading unit to be discharged into Trimethylamine 99 basin and oxyethane basin respectively raw material Trimethylamine 99 and oxyethane; (2) raw material Trimethylamine 99 and hydrochloric acid are sent into from Trimethylamine 99 basin and hydrochloric acid basin respectively carried out building-up reactions in the single step reaction synthesis tank and generate the intermediate trimethylamine hydrochloride; (3) trimethylamine hydrochloride and oxyethane are fed respectively send into the reaction of two steps reaction synthesis tank in the test tank after the metering and generate the crude product choline chloride 60, the crude product choline chloride 60 is sent into the choline chloride 60 basin; (4) the crude product choline chloride 60 is concentrated through concentrating unit, decolorizing with activated carbon, after filtering, further produces flame filter press the choline chloride 60 liquid of different concns, or drying obtains pulvis choline chloride 60 product after adding the vehicle figuration, it is characterized in that, the raw material Trimethylamine 99 in the described step (1) and the unloading unit of oxyethane are the airtight volatilization prevention unloading unit of clean, this device has the Trimethylamine 99 hydrogen pump that the compressor that uses or oxyethane unloads and use of unloading, compressed machine of gas that evaporating in Trimethylamine 99 or the oxyethane basin produces or hydrogen pump compression back feed tank car, cause the tank car internal pressure to raise, liquid in the tank car flows into Trimethylamine 99 or oxyethane basin through liquid-phase tube under the effect of pressure, thereby reached cleaning, airtight purpose of unloading, hydrochloric acid basin in Trimethylamine 99 basin in the described step (1) and oxyethane basin and the step (2) all is a kind of basin with magnetic turn-over liquid level display unit, can in time observe a jar interior liquid level by the magnetic turn-over liquidometer, single step reaction synthesis tank in the described step (2) is a kind of synthesis tank that has the suitable choline chloride 60 chemosynthesis of recycle pump and graphite heat exchanger, when carrying out the choline chloride 60 chemosynthesis, earlier hydrochloric acid is fed the single step reaction synthesis tank, ON cycle pump then, again Trimethylamine 99 is slowly fed the single step reaction synthesis tank, feed liquid from single step reaction synthesis tank bottom after pipeline enters recycle pump and mixes rapidly, again after pipeline enters the interchanger cooling, return the single step reaction synthesis tank again, thereby reach the purpose that makes feed liquid mix and prevent the feed liquid local superheating rapidly, concentrating unit in the described step (4) has circular hole graphite heat exchanger and separator, crude product choline chloride 60 material enters in the separator by pipeline after the heating of circular hole graphite heat exchanger concentrates, a part of material in the separator is got back to the circular hole graphite heat exchanger through circulating line and is proceeded to concentrate, and rest materials flows out from discharge port.
Can also be provided with pressure equaliser on the tank body of the single step reaction synthesis tank in described rapid (2), described pressure equaliser comprises intermediate receptacle, equilibration tube, reflux and return line, when the tank body internal pressure raises, pot liquid rises along equilibration tube, when liquid surpasses the equilibration tube height, liquid will rise to intermediate receptacle from equilibration tube, enters reflux through return line again, guarantees that the tank body internal pressure is no more than prescribed value.
Hydrochloric acid basin in the described step (2), Trimethylamine 99 basin and single step reaction synthesis tank can also link to each other with the clean gas concentration unit, in process of production gas of Chan Shenging and the gas that in unloading the process of Trimethylamine 99, produces respectively the water in one-level, secondary, tertiary filter enter the recycle of single step reaction synthesis tank again after absorbing.
The invention has the beneficial effects as follows: production technology for choline chloride of the present invention has not only improved production capacity, has reduced energy consumption, and has reduced environmental pollution, has guaranteed the quality of choline chloride 60.Single step reaction synthesis tank, the concentrating unit of the airtight volatilization prevention unloading unit of basin, clean of the band magnetic turn-over liquidometer that adopts, gas concentration unit, supporting metering system apparatus, suitable choline chloride 60 have satisfied mass-produced demand, improved production capacity greatly, reduced the discharging of the three wastes, reduce energy consumption, guaranteed quality product.
Description of drawings
Fig. 1 is a process flow diagram of the present invention.
Fig. 2 is the structured flowchart of the airtight volatilization prevention unloading unit of clean, 1, escape pipe, 2, compressor (hydrogen pump), 3, inlet pipe, 4, basin, 5, liquid-phase tube, 6, tank car.
Fig. 3 is the structured flowchart of the basin of band magnetic turn-over liquid level display unit, 1, tank body, 2, the gas connecting leg, 3, gas connecting leg valve, 4, stainless steel tube, 5, the magnet ball, 6, the float of carry magnet, 7, the evacuated tube valve, 8, evacuated tube, 9, liquid connecting leg valve, 10, the liquid connecting leg.
Fig. 4 is the structure iron of single step reaction synthesis tank, 1, tank body, 2, the Trimethylamine 99 import, 3, the hydrochloric acid import, 4, circulation tube, 5, water outlet, 6, interchanger, 7, water-in, 8, second valve, 9, outlet valve, 10, thief hole valve, 11, thief hole, 12, recycle pump, 13, first valve.
Fig. 5 is equipped with the structured flowchart of the test tank of weighbridge for the bottom, and 1, tank body, 2, display unit, 3, measuring apparatus.
Fig. 6 is the structured flowchart of concentrating unit, 1, discharge nozzle, 2, steam inlet, 3, nahlock hole graphite heat exchanger, 4, water outlet, 5, the charging valve, 6, feed-pipe, 7, venting port, 8, separator, 9, the natural circulation pipe, 10, separate discharge nozzle, 11, basin.
Fig. 7 is the structured flowchart of pressure equaliser, 1, return line, 2, reflux, 3, ventilating pit, 4, intermediate receptacle, 5, equilibration tube, 6, tank body.
Fig. 8 is the structured flowchart of clean gas concentration unit, 1, hydrochloric acid tank, 2, the Trimethylamine 99 jar, 3, synthesis tank, 4, vacuum pump, 5, grade one filter, 6, secondary filter, 7, tertiary filter, 8, tank body, 9, impeller pump.
Embodiment
As shown in Figure 1, choline chloride 60 process implementing mode of the present invention is:
(1) utilize the airtight volatilization prevention unloading unit of clean shown in Figure 2 to be discharged into the Trimethylamine 99 basin and the oxyethane basin of band magnetic turn-over liquid level display unit as shown in Figure 3 respectively raw material Trimethylamine 99 and oxyethane;
(2) raw material Trimethylamine 99 and hydrochloric acid are carried out building-up reactions generation intermediate trimethylamine hydrochloride respectively in Trimethylamine 99 basin and hydrochloric acid basin (as shown in Figure 3 with magnetic turn-over liquid level display unit) feeding suitable choline chloride 60 synthetic single step reaction synthesis tank as shown in Figure 4; Jar internal pressure that prevents that the tank body of described single step reaction synthesis tank is provided with as shown in Figure 7 surpasses the pressure equaliser of prescribed value; Described hydrochloric acid basin, Trimethylamine 99 basin and single step reaction synthesis tank all link to each other with as shown in Figure 8 clean gas concentration unit, in process of production gas of Chan Shenging and the gas that in unloading the process of Trimethylamine 99, produces respectively in one-level, secondary, tertiary filter clear water enter the recycle of single step reaction synthesis tank again after absorbing;
(3) trimethylamine hydrochloride is fed the test tank that as shown in Figure 5 bottom is equipped with weighbridge, measure the weight of the trimethylamine hydrochloride of one-step synthesis generation by test tank, calculate the amount of the required oxyethane of two step building-up reactionss then according to the weight of trimethylamine hydrochloride, again oxyethane feeding bottom as shown in Figure 5 is equipped with another test tank of weighbridge, measure the required oxyethane of two step building-up reactionss, again the trimethylamine hydrochloride and the oxyethane that measure are sent into two steps reaction synthesis tank reaction generation crude product choline chloride 60, the crude product choline chloride 60 is sent into the choline chloride 60 basin;
(4) with the crude product choline chloride 60 through the choline chloride 60 liquid that as shown in Figure 6 the distillation concentrating unit that comprises nahlock hole graphite heat exchanger, separator and basin concentrates, decolorizing with activated carbon, flame filter press are further produced different concns after filtering, or drying obtains pulvis choline chloride 60 product after adding the vehicle figuration.
The airtight volatilization prevention unloading unit of clean of the present invention among Fig. 2, its structure comprises basin 4 and compressor (hydrogen pump) 2, described basin 4 links to each other with the gas phase import of compressor (hydrogen pump) 2 by inlet pipe 3, the gaseous phase outlet of compressor 2 links to each other with tank car 6 by escape pipe 1, and described tank car 6 links to each other by liquid-phase tube 5 with basin 4.When unloading; open compressor (hydrogen pump) 2; the compressed machine of gas (hydrogen pump) 2 compression backs in the basin 4 feed tank car 6, cause tank car 6 internal pressures to raise, and the liquid in the tank car 6 flows into basin 4 through liquid-phase tube 5 under the effect of pressure; thereby finish unloading of Trimethylamine 99 (oxyethane); whole process is airtight work, and no gas is excessive, has both avoided the waste of Trimethylamine 99 (oxyethane); protect environment again, improved safety factors.
Fig. 3 is the basin of band liquid level display unit of the present invention, its structure comprises tank body 1, side at tank body 1 is provided with the liquid level display unit, described liquid level display unit is the magnetic turn-over liquidometer, the magnetic turn-over liquidometer comprises stainless steel tube 4, the float 6 of magnet ball 5 and carry magnet, stainless steel tube 4 sealing two ends, described magnet ball 5 is arranged on the outside of stainless steel tube 4, the float 6 of carry magnet is arranged in the stainless steel tube 4, the bottom of stainless steel tube 4 is provided with the evacuated tube 8 that has evacuated tube valve 7, the upper and lower of described stainless steel tube 4 is connected with tank body 1 by gas connecting leg 2 and liquid connecting leg 10 respectively, described gas connecting leg 2 is provided with gas connecting leg valve 3, and liquid connecting leg 10 is provided with liquid connecting leg valve 9.During use, open gas connecting leg valve 3 and liquid connecting leg valve 9, when the liquid level in the tank body 1 rose, the liquid level in the stainless steel tube 4 also can be along with rising, and is the same high with liquid level in the tank body 1, thereby the float of carry magnet 6 also can be along with rising, when the float 6 of carry magnet rose, the magnet ball 5 of stainless steel tube 4 outsides was subjected to the magneticaction of inner float 6, stirs, two kinds of colors of magnet ball 5 usefulness are coated with notes, and 5 two kinds of color intersections of magnet ball are the liquid level of liquid in the tank body 1.
Fig. 4 is a reaction synthesis tank of the present invention, its structure comprises tank body 1, described tank body 1 is acidproof, alkali, the horizontal type structure that pyritous special glass steel matter is made, the top of tank body 1 is provided with Trimethylamine 99 import 2 and hydrochloric acid import 3, the right side of tank body 1 is connected with circulation tube 4, the other end of circulation tube 4 is connected with the top of tank body 1, described circulation tube 4 is provided with recycle pump 12 and interchanger 6, the left side of recycle pump 12 is provided with first valve 13, the right side is provided with a thief hole 11 that has a thief hole valve 10, the upper right of thief hole 11 is provided with outlet valve 9, the circulation tube 4 on thief hole 11 tops is provided with second valve 8, described interchanger 6 is the graphite tubular heat exchange, and the top of interchanger 6 is provided with water outlet 5, and the bottom is provided with water-in 7.When carrying out the choline chloride 60 chemosynthesis, earlier squeeze into a certain amount of hydrochloric acid from the hydrochloric acid import 3 on tank body 1 top with pump, ON cycle pump 12, slowly open Trimethylamine 99 again and feed valve, feed Trimethylamine 99 from the Trimethylamine 99 import 2 on tank body 1 top, open first valve 13 and second valve 8, close thief hole valve 10 and outlet valve 9, liquid is lowered the temperature through graphite tubular heat exchange 6 through recycle pump 12 circulations; When synthetics is taken a sample, close second valve 8 and outlet valve 9, open first valve 13 and thief hole valve 10, can take a sample; When reaction is finished, close second valve 8 and thief hole valve 10, open first valve 13 and outlet valve 9, reactant can be discharged.
Fig. 5 is a kind of production test tank of the present invention, and its structure comprises tank body 1, and the bottom of tank body 1 is provided with the measuring apparatus 3 that has display unit 2.Described tank body 1 is the intermediate jar, and measuring apparatus 3 is the frame-type weighbridge, and described intermediate jar is used to place trimethylamine hydrochloride; Described tank body 1 is the oxyethane jar, and measuring apparatus 3 is small-sized weighbridge.Described oxyethane jar is used to place raw material oxyethane.During use, by the weight that the frame-type weighbridge measures the trimethylamine hydrochloride of one-step synthesis generation, the weight of needed oxyethane when synthesizing by small-sized two steps of weighbridge metering.
Fig. 6 is a concentrating unit of the present invention, its structure comprises nahlock hole graphite heat exchanger 3, separator 8 and basin 11, the top of described nahlock hole graphite heat exchanger 3 is provided with steam inlet 2, the bottom is provided with water outlet 4, the bottom is provided with the feed-pipe 6 that has charging valve 5, the top is connected with discharge nozzle 1, the other end of discharge nozzle 1 links to each other with separator 8, the top of separator 8 is provided with venting port 7, the bottom is provided with natural circulation pipe 9, the other end of natural circulation pipe 9 links to each other with the bottom of nahlock hole graphite heat exchanger 3, and the separator 8 of described discharge nozzle 1 bottom is provided with and separates discharge nozzle 10, separates discharge nozzle 10 and extend into basin 11 bottoms.When material need concentrate, steam enters from the steam inlet 2 of nahlock hole graphite heat exchanger 3, water outlet 4 places in bottom discharge water of condensation, open charging valve 5, material enters from the feed-pipe 6 of graphite heat exchanger 3 bottoms, nahlock hole, the steam that enters in the nahlock hole graphite heat exchanger 3 heats concentrated to material, material enters in the separator 8 along discharge nozzle 1, part material enters in the natural circulation pipe 9, its clout enters into basin 11 bottoms along separating discharge nozzle 10, gas in the separator 8 is discharged circulation connection work from venting port 7; When needs quit work; close charging valve 5, the temperature in the nahlock hole graphite heat exchanger 3 is also very high at this moment, carries out natural circulation by the materials in the natural circulation pipe 9; come nahlock hole graphite heat exchanger 3 is lowered the temperature, thereby protection nahlock hole graphite heat exchanger 3 can be not overheated and damage.
Fig. 7 is a kind of pressure equaliser, its structure comprises intermediate receptacle 4, equilibration tube 5, reflux 2 and return line 1, the top of intermediate receptacle 4 is provided with ventilating pit 3 and communicates with it, the bottom is provided with equilibration tube 5 and the return line 1 that is connected, the bottom of described return line 1 is provided with reflux 2, and the bottom of described equilibration tube 5 extend into the bottom of tank body 6.Pressure in tank body 6 raises, and then jar interior 6 liquid rise along equilibration tube 5, if surpass the level pressure value of equilibration tube 5, liquid will rise to intermediate receptacle 4 from equilibration tube 5, enters reflux 2 through return line 1 again, guarantees that tank body 6 internal pressures are no more than prescribed value.After synthetic the finishing, send liquid and downtime outside when being subjected to the variation of envrionment temperature, be easy to generate negative pressure in the tank body 6, if generate negative pressure, air then enters from ventilating pit 3, enters in the tank body 6 along equilibration tube 5, plays the effect of protection tank body 6.
Fig. 8 is the clean gas concentration unit, its structure comprises grade one filter 5, secondary filter 6, tertiary filter 7, vacuum pump 4 and impeller pump 9, described grade one filter 5 is by impeller pump 9, vacuum pump 4 and gas pipeline respectively with hydrochloric acid tank 1, Trimethylamine 99 jar 2 links to each other with synthesis tank 3, the gas pipeline at grade one filter 5 tops enters into the bottom of secondary filter 6, the gas pipeline at secondary filter 6 tops enters into the bottom of tertiary filter 7, the gas pipeline at tertiary filter 7 tops communicates with atmosphere, the bottom of tertiary filter 7 and secondary filter 6 links to each other with grade one filter 5 bottoms by fluid pipeline respectively, and grade one filter 5 enters in tank body 8 and the synthesis tank 3 by fluid pipeline.The gas of Chan Shenging in process of production, through vacuum pump 4 and impeller pump 9 gas is mixed by gas pipeline with the gas that in unloading the process of Trimethylamine 99, produces in grade one filter 5 with clear water, the air pressure that in grade one filter 5, is produced like this, gas pipeline by grade one filter 5 tops is pressed into secondary filter 6 bottoms, absorb through clear water again, the gas that produced this moment, gas pipeline by secondary filter 6 tops is pressed into tertiary filter 7 bottoms, once more behind the clear water absorbing and filtering, gas pipeline high altitude discharge through tertiary filter 7 tops, after reaching finite concentration, the clear water concentration in the grade one filter 5 enters in the tank body 8, enter into again in the workshop synthesis tank 3 and use, water in secondary filter 6 and the tertiary filter 7 enters in the grade one filter 5, then mend in secondary filter 6 and the tertiary filter 7, remain institute's discharging waste gas qualified discharge to new water.
Claims (3)
1. the production technique of a choline chloride 60, may further comprise the steps: (1) utilizes the raw material unloading unit to be discharged into Trimethylamine 99 basin and oxyethane basin respectively raw material Trimethylamine 99 and oxyethane; (2) raw material Trimethylamine 99 and hydrochloric acid are sent into from Trimethylamine 99 basin and hydrochloric acid basin respectively carried out building-up reactions in the single step reaction synthesis tank and generate the intermediate trimethylamine hydrochloride; (3) trimethylamine hydrochloride and oxyethane are fed respectively send into the reaction of two steps reaction synthesis tank in the test tank after the metering and generate the crude product choline chloride 60, the crude product choline chloride 60 is sent into the choline chloride 60 basin; (4) the crude product choline chloride 60 is concentrated through concentrating unit, decolorizing with activated carbon, after filtering, further produces flame filter press the choline chloride 60 liquid of different concns, or drying obtains pulvis choline chloride 60 product after adding the vehicle figuration, it is characterized in that, the raw material Trimethylamine 99 in the described step (1) and the unloading unit of oxyethane are the airtight volatilization prevention unloading unit of clean, this device has the Trimethylamine 99 hydrogen pump that the compressor that uses or oxyethane unloads and use of unloading, compressed machine of gas that evaporating in Trimethylamine 99 or the oxyethane basin produces or hydrogen pump compression back feed tank car, cause the tank car internal pressure to raise, liquid in the tank car flows into Trimethylamine 99 or oxyethane basin through liquid-phase tube under the effect of pressure, thereby reached cleaning, airtight purpose of unloading, hydrochloric acid basin in Trimethylamine 99 basin in the described step (1) and oxyethane basin and the step (2) all is a kind of basin with magnetic turn-over liquid level display unit, can in time observe a jar interior liquid level by the magnetic turn-over liquidometer, single step reaction synthesis tank in the described step (2) is a kind of synthesis tank that has the suitable choline chloride 60 chemosynthesis of recycle pump and graphite heat exchanger, when carrying out the choline chloride 60 chemosynthesis, earlier hydrochloric acid is fed the single step reaction synthesis tank, ON cycle pump then, again Trimethylamine 99 is slowly fed the single step reaction synthesis tank, feed liquid from single step reaction synthesis tank bottom after pipeline enters recycle pump and mixes rapidly, again after pipeline enters the interchanger cooling, return the single step reaction synthesis tank again, thereby reach the purpose that makes feed liquid mix and prevent the feed liquid local superheating rapidly, concentrating unit in the described step (4) has circular hole graphite heat exchanger and separator, crude product choline chloride 60 material enters in the separator by pipeline after the heating of circular hole graphite heat exchanger concentrates, a part of material in the separator is got back to the circular hole graphite heat exchanger through circulating line and is proceeded to concentrate, and rest materials flows out from discharge port.
2. the production technique of a kind of choline chloride 60 as claimed in claim 1, it is characterized in that, the tank body of the single step reaction synthesis tank in the described step (2) is provided with pressure equaliser, described pressure equaliser comprises intermediate receptacle, equilibration tube, reflux and return line, when the tank body internal pressure raise, pot liquid rose along equilibration tube, when liquid surpasses the equilibration tube height, liquid will rise to intermediate receptacle from equilibration tube, enters reflux through return line again.
3. the production technique of a kind of choline chloride 60 as claimed in claim 1 or 2, it is characterized in that, hydrochloric acid basin in the described step (2), Trimethylamine 99 basin and single step reaction synthesis tank link to each other with the clean gas concentration unit, in process of production gas of Chan Shenging and the gas that in unloading the process of Trimethylamine 99, produces respectively the water in one-level, secondary, tertiary filter enter the recycle of single step reaction synthesis tank again after absorbing.
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| Application Number | Priority Date | Filing Date | Title |
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| CN2009102292338A CN101691333B (en) | 2009-10-21 | 2009-10-21 | Production technology for choline chloride |
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| CN2009102292338A CN101691333B (en) | 2009-10-21 | 2009-10-21 | Production technology for choline chloride |
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| CN101691333B CN101691333B (en) | 2012-07-25 |
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102702304A (en) * | 2012-05-11 | 2012-10-03 | 中南大学 | Multipath pre-activating device, peptide nucleic acid preparation system, and pre-activating and synthetizing method |
| CN103044265A (en) * | 2012-12-21 | 2013-04-17 | 聊城盐杉新材料科技有限公司 | Device and method for producing high-concentration trimethylamine hydrochloride |
| CN104460730A (en) * | 2014-05-21 | 2015-03-25 | 河北碧隆化工科技有限公司 | PH value control method in choline chloride production process |
| CN105198761A (en) * | 2015-10-20 | 2015-12-30 | 山东恩贝科技有限公司 | Crystal with high content of choline chloride and preparation method of crystal |
| CN107572152A (en) * | 2017-09-18 | 2018-01-12 | 京东方科技集团股份有限公司 | A kind of fluid storage device |
| CN109277062A (en) * | 2018-10-16 | 2019-01-29 | 绍兴东湖高科股份有限公司 | Microchannel reaction unit and the method for preparing choline chloride using microchannel |
| WO2023123525A1 (en) * | 2021-12-29 | 2023-07-06 | 山东天成万丰投资有限公司 | Device for recycling tail gas from choline chloride production |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| NL127406C (en) * | 1964-11-04 | |||
| DD241595B1 (en) * | 1985-10-04 | 1990-06-20 | Chemisch Pharmazeutisches Werk | METHOD AND DEVICE FOR PREPARING CHOLIN CHLORIDE |
| CN1078231A (en) * | 1992-05-02 | 1993-11-10 | 中国石油化工总公司上海石油化工总厂 | The manufacture method of choline chloride 60 |
-
2009
- 2009-10-21 CN CN2009102292338A patent/CN101691333B/en active Active
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102702304A (en) * | 2012-05-11 | 2012-10-03 | 中南大学 | Multipath pre-activating device, peptide nucleic acid preparation system, and pre-activating and synthetizing method |
| CN103044265A (en) * | 2012-12-21 | 2013-04-17 | 聊城盐杉新材料科技有限公司 | Device and method for producing high-concentration trimethylamine hydrochloride |
| CN104460730A (en) * | 2014-05-21 | 2015-03-25 | 河北碧隆化工科技有限公司 | PH value control method in choline chloride production process |
| CN104460730B (en) * | 2014-05-21 | 2016-08-24 | 河北碧隆化工科技有限公司 | Method of pH control in choline chloride production process |
| CN105198761A (en) * | 2015-10-20 | 2015-12-30 | 山东恩贝科技有限公司 | Crystal with high content of choline chloride and preparation method of crystal |
| CN107572152A (en) * | 2017-09-18 | 2018-01-12 | 京东方科技集团股份有限公司 | A kind of fluid storage device |
| CN107572152B (en) * | 2017-09-18 | 2019-01-11 | 京东方科技集团股份有限公司 | A kind of fluid storage device |
| CN109277062A (en) * | 2018-10-16 | 2019-01-29 | 绍兴东湖高科股份有限公司 | Microchannel reaction unit and the method for preparing choline chloride using microchannel |
| WO2023123525A1 (en) * | 2021-12-29 | 2023-07-06 | 山东天成万丰投资有限公司 | Device for recycling tail gas from choline chloride production |
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|---|---|
| CN101691333B (en) | 2012-07-25 |
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