Production system of sodium methyl taurate
By using Zr-modified HZSM-5 catalyst and an optimized production process, the problems of rapid catalyst activity reduction and high energy consumption were solved, achieving low-cost, high-efficiency production of sodium methyl taurate with fewer byproducts and a longer catalyst life.
Patent Information
- Application Number
- CN202511590935.4
- Authority / Receiving Office
- CN · China
- Patent Type
- Applications(China)
- Current Assignee / Owner
- Filing Date
- 2025-11-03
- Publication Date
- 2026-01-23
AI Technical Summary
In the existing sodium methyl taurate production process, the catalyst activity decreases rapidly, the cost is high, the high-pressure reaction equipment has high energy consumption, and there are many by-products, making it difficult to achieve efficient and low-cost production.
Using Zr-modified HZSM-5 catalyst, multi-level pores were formed by controlling the pore structure with PEG and combined with steam-assisted crystallization. The resulting catalyst exhibited high selectivity and long lifespan in the pressurized preparation of sodium methyl taurate. Furthermore, by recycling methylamine, a high-pressure reactor and a shell-and-tube heat exchanger were designed to optimize the production process.
This technology enables the efficient production of sodium methyl taurate, reduces production costs, minimizes byproducts, extends catalyst lifespan, and improves production efficiency.
Smart Images
Figure CN121372237A_ABST
Abstract
Description
Technical Field
[0001] This invention relates to the field of sodium methyl taurate technology, and particularly to a production system for sodium methyl taurate. Background Technology
[0002] Sodium methyltaurate is a high-performance, mild anionic surfactant. With its low irritation, good compatibility, and rich foam, it has become an indispensable core ingredient in high-end daily chemical products, especially those for sensitive skin and infant care. Simultaneously, sodium methyltaurate is also an important intermediate in pharmaceutical synthesis and a biochemical reagent.
[0003] The preparation methods of sodium methyl taurate mainly include the direct method and the pressure method. The direct method involves a nucleophilic substitution reaction between methylamine and sodium chloroethanesulfonate under alkaline conditions to produce sodium methyl taurate. Its advantages are a direct route and readily available raw materials. Disadvantages include the higher cost of sodium chloroethanesulfonate and the need for alkali neutralization of the hydrogen chloride generated during the reaction, resulting in a significant amount of inorganic salt byproducts. The pressure method involves a dehydration reaction between methylamine and sodium hydroxyethanesulfonate under high temperature and pressure to produce sodium methyl taurate. Its advantages include fewer byproducts and better adherence to green chemistry principles. Disadvantages include the large size of the high-pressure reaction equipment and higher energy consumption. The pressure method is an advanced and environmentally friendly process for producing sodium methyl taurate. Although the initial investment in equipment and safety is higher, its route is cleaner and the product quality is better. The pressure method requires a catalyst, with mainstream catalysts being metal oxide catalysts and molecular sieve catalysts. Metal oxide catalysts such as alumina and calcium oxide are inexpensive and readily available, but alumina may undergo a phase transition under hydrothermal conditions, and calcium oxide has relatively low activity and may continuously leach out in the aqueous phase. Molecular sieve catalysts have the advantages of high activity and good selectivity, but they are expensive. Although the catalyst does not participate in the chemical reaction during use, its activity will inevitably decrease with the extension of the service time, requiring regeneration or replacement with a new batch of catalyst. Summary of the Invention
[0004] The purpose of this invention is to provide a production system for sodium methyl taurate that has the effect of a catalyst.
[0005] The above-mentioned technical objective of the present invention is achieved through the following technical solution: a production system for sodium methyl taurate, comprising a raw material storage tank system, a preheater, a reactor, a cooler connected to the reactor, a flash tank connected to the cooler, a methylamine recovery system connected to the flash tank, and a purification and refining system. The raw material storage tank system includes a methylamine storage tank, a sodium hydroxyethyl sulfonate solution storage tank, and a catalyst storage container. The methylamine storage tank contains methylamine, the sodium hydroxyethyl sulfonate solution storage tank contains sodium hydroxyethyl sulfonate solution, and the catalyst storage tank contains Zr-modified HZSM-5 catalyst.
[0006] By adopting the above technical solution, the raw material storage tank system is used to store raw materials. The methylamine storage tank needs to be designed as a pressure tank, equipped with insulation, cooling, and safety valves, for storing liquid methylamine. The sodium hydroxyethyl sulfonate solution storage tank is used to store sodium hydroxyethyl sulfonate solution. The catalyst storage tank is used to store new catalyst or regenerated catalyst.
[0007] The preheater is used to preheat the raw materials before they enter the reactor, bringing them close to the reaction temperature.
[0008] The reactor is a key piece of equipment in the production system, serving as a pressure vessel and providing a site for chemical reactions. After the reaction, the high-temperature, high-pressure materials enter a cooler for rapid cooling, terminating the reaction and preparing for subsequent flash evaporation and separation.
[0009] The rapidly cooled material enters the flash tank, which is designed as a medium-to-low pressure vessel. Inside the flash tank, the pressure drops rapidly, and excess, unreacted methylamine in the material instantly vaporizes, separating from the liquid products. The vaporized methylamine enters the methylamine recovery system, where it is recovered and reused as a raw material in the chemical reaction within the reactor, thus achieving recycling, reducing costs, and being environmentally friendly.
[0010] The liquid material in the flash tank enters the purification and refining system for purification and refining to obtain sodium methyl taurate as the finished product.
[0011] A further configuration of the present invention is as follows: the reactor is a high-pressure reactor, the high-pressure reactor is equipped with a magnetically driven stirrer, and the cooler is a shell-and-tube heat exchanger.
[0012] By adopting the above technical solution, the high-pressure reactor is suitable for batch production and is equipped with a magnetically driven stirrer to ensure the sealing performance of the dynamic seal under high pressure. The cooler is a shell-and-tube heat exchanger, which can rapidly cool the high-temperature and high-pressure materials after the reaction.
[0013] A further provision of the present invention is that: a feed pipeline is provided between the sodium hydroxyethyl sulfonate solution storage tank and the reactor; the methylamine storage tank is a pressure storage tank; a feed pipeline is installed between the methylamine storage tank and the reactor; and both the feed pipeline and the feed pipeline are equipped with high-pressure plunger pumps.
[0014] By adopting the above technical solution, the two high-pressure plunger pumps on feed line one and feed line two are used to pump methylamine and sodium hydroxyethyl sulfonate into the precooler and reactor, respectively.
[0015] A further feature of the present invention is that the flash tube comprises a vertical tank.
[0016] A further embodiment of the present invention is that the methylamine recovery system includes a compressor, a methylamine condenser, and a methylamine temporary storage tank, wherein the methylamine temporary storage tank is connected to the methylamine storage tank via a pipeline.
[0017] By adopting the above technical solution, the compressor is used to compress and liquefy the low-pressure methylamine gas that has flashed out, increasing the pressure for recovery. The methylamine condenser is used to condense the compressed high-temperature methylamine gas into a liquid state, and the methylamine storage tank is used to temporarily store the recovered liquid methylamine.
[0018] A further provision of the present invention is that the purification and refining system includes a decolorization tank, the decolorization tank is equipped with a stirrer and a heating jacket, and the decolorization tank is filled with activated carbon.
[0019] By adopting the above technical solution, the decolorizing tank is filled with activated carbon to adsorb colored impurities in the liquid material, and the stirrer is used to stir the liquid material.
[0020] A further embodiment of the present invention is that the purification and refining system further includes a filtration device, an evaporation and concentration device, a crystallization tank, a solid-liquid separation device, and a drying device.
[0021] By adopting the above technical solution, the filtration equipment is used to filter and remove residual activated carbon powder and trace insoluble matter from the material, obtaining a clear filtrate. The filtrate is then concentrated in an evaporation and concentration device to reduce moisture content, preparing for the next crystallization step. The concentrated liquid crystallizes in a crystallization tank, and sodium methyl taurate crystallizes out from the supersaturated solution. Through a solid-liquid separation device, solid sodium methyl taurate is obtained. The solid sodium methyl taurate is then dried in a drying device to obtain sodium methyl taurate.
[0022] A further provision of the present invention is that the evaporation and concentration device is a vacuum evaporator, and the solid-liquid separation device is a centrifuge.
[0023] A further provision of the present invention is as follows: The Zr-modified HZSM-5 catalyst is prepared as follows: TEOS, TPAOH, aluminum isopropoxide, deionized water, PEG, and Zr(NO3)4▪5H2O are weighed according to the molar ratio of SiO2:Al2O3:TPAOH:H2O:PEG:Zr(NO3)4▪5H2O = 1:0.01:0.3:50:0.01:0.01, and stirred evenly at 60°C to obtain a dry gel. After cooling to 15-25℃ and standing for 24 hours, the catalyst was baked at 155-160℃ for 27 hours in a sealed container under water vapor conditions. After washing with water until neutral, it was dried at 100℃, dissolved and recrystallized in TPAOH / NaOH solution, washed with water until neutral, dried at 100℃ for 8 hours, calcined at 550℃ for 6 hours, cooled, and then treated with 1.5 mol / L ammonium chloride solution for ion exchange at 60℃. After drying, the Zr-modified HZSM-5 catalyst was obtained.
[0024] By adopting the above technical solution, the HZSM-5 catalyst exhibits excellent hydrothermal stability among molecular sieve catalysts. In practice, its pore structure and acidic sites demonstrate good selectivity when applied to the pressurized preparation process of sodium methyltaurate. However, the cost of HZSM-5 catalyst is relatively high. To further extend the service life of HZSM-5 catalyst and reduce the production cost of sodium methyltaurate, modification treatment of HZSM-5 catalyst is necessary. In existing technologies, the modification of molecular sieve catalysts is mostly carried out by impregnation, but the metal loaded by impregnation has the disadvantage of easy loss of active sites and poor cycle stability. Through research, this invention uses PEG to regulate the pore structure of the molecular sieve to form a hierarchical pore structure. After water vapor-assisted crystallization forms a mesoporous structure, the selectivity can be improved. At the same time, the newly added Zr sites are not loaded by impregnation but added during the catalyst preparation process. The resulting catalyst has good selectivity, long life, and good cycle stability.
[0025] The beneficial effects of this invention are: the invention supplies raw materials through a raw material storage tank system, methylamine and sodium hydroxyethyl sulfonate undergo a chemical reaction in the reactor, and the reacted materials are processed through a flash tank, purification and refining system to obtain sodium methyl taurate. There are few reaction byproducts. The production cost of sodium methyl taurate is reduced by recycling methylamine and using Zr-modified HZSM-5 catalyst with long service life and good cycle stability. Attached Figure Description
[0026] Figure 1 This is a system schematic diagram of the present invention. Detailed Implementation
[0027] Example: A production system for sodium methyl taurate, such as Figure 1 The system includes a raw material storage tank system, a preheater, a reactor, a cooler connected to the reactor, a flash tank connected to the cooler, a methylamine recovery system connected to the flash tank, and a purification and refining system. The raw material storage tank system includes a methylamine storage tank, a sodium hydroxyethyl sulfonate solution storage tank, and a catalyst storage container. The methylamine storage tank contains methylamine, the sodium hydroxyethyl sulfonate solution storage tank contains sodium hydroxyethyl sulfonate solution, and the catalyst storage tank contains Zr-modified HZSM-5 catalyst for replacing the catalyst in the reactor. A feed line one is provided between the sodium hydroxyethyl sulfonate solution storage tank and the reactor. The methylamine storage tank is a pressure tank, and a second feed line two is installed between the methylamine storage tank and the reactor. Both feed lines one and two are equipped with high-pressure plunger pumps.
[0028] The reactor is a high-pressure reactor equipped with a magnetically driven stirrer and contains a Zr-modified HZSM-5 catalyst. The cooler is a shell-and-tube heat exchanger. The flash tank is a vertical tank.
[0029] The methylamine recovery system includes a compressor, a methylamine condenser, and a methylamine temporary storage tank, which is connected to the methylamine storage tank via pipelines.
[0030] The purification and refining system includes a decolorization tank, filtration equipment, an evaporation and concentration unit, a crystallization tank, a solid-liquid separation unit, and a drying unit. The decolorization tank is equipped with a stirrer and a heating jacket, and contains activated carbon. The evaporation and concentration unit is a vacuum evaporator, and the solid-liquid separation unit is a centrifuge.
[0031] The preparation method of Zr-modified HZSM-5 catalyst is as follows: TEOS, TPAOH, aluminum isopropoxide, deionized water, PEG, and Zr(NO3)4▪5H2O were weighed according to the molar ratio of SiO2:Al2O3:TPAOH:H2O:PEG:Zr(NO3)4▪5H2O = 1:0.01:0.3:50:0.01:0.01. The mixture was stirred evenly at 60℃ to obtain a dry gel, which was then cooled to 15℃. After standing at 25℃ for 24 hours, it was baked at 155-160℃ for 27 hours in a sealed container under water vapor environment. After washing with water until neutral, it was dried at 100℃, dissolved and recrystallized in TPAOH / NaOH solution, washed with water until neutral, dried at 100℃ for 8 hours, calcined at 550℃ for 6 hours, cooled, and then treated with 1.5 mol / L ammonium chloride solution for ion exchange at 60℃. After drying, Zr-modified HZSM-5 catalyst was obtained.
[0032] Comparative Example 1: A production system for sodium methyl taurate, which differs from the examples in that the catalyst used is HZSM-5 catalyst.
[0033] Comparative Example 2: A production system for sodium methyl taurate, differing from the examples in that the catalyst is prepared as follows: TEOS, TPAOH, aluminum isopropoxide, deionized water, PEG, and Zr(NO3)4▪5H2O are weighed according to the molar ratio of SiO2:Al2O3:TPAOH:H2O:PEG:Zr(NO3)4▪5H2O = 1:0.01:0.3:50:0.01:0.01, and stirred evenly at 60°C to obtain... The gel was dried, cooled to 15-25℃, and allowed to stand for 24 hours. It was then baked at 155-160℃ for 27 hours in a sealed container under steam. After washing with water until neutral, it was dried at 100℃, dissolved and recrystallized in TPAOH / NaOH solution, washed with water until neutral, dried at 100℃ for 8 hours, calcined at 550℃ for 6 hours, cooled, and then subjected to ion exchange treatment in 1.5 mol / L ammonium chloride solution at 60℃. After drying, Zr-modified HZSM-5 catalyst was obtained. HZSM-5 catalyst and Zr(NO3)4▪5H2O were added to deionized water, stirred vigorously under ultrasonic conditions for 1 hour, and evaporated under reduced pressure to obtain powder. After drying for 12 hours, it was calcined at 550℃ for 6 hours to obtain Zr-modified HZSM-5 catalyst obtained by impregnation.
[0034] Experimental section: Process parameters: Reactor temperature: 200-220℃, pressure: 4MPa, reaction time: 1h.
[0035] Methyl taurine was produced in Examples 1 and 2 and Comparative Examples 1-2 according to the above process parameters. The yield of each batch was measured at 24h, 48h, 72h, and 96h, with results shown in Table 1. It can be seen that the lifetime of the Zr-modified HZSM-5 catalyst in the examples was significantly increased.
[0036] Table 1. Yields of the batches in Examples 1 and 2 at the corresponding time points.
Claims
1. A production system of sodium methyl taurate, characterized by: The application relates to a methylamine production system, which comprises a raw material storage tank system, a preheater, a reactor, a cooler connected with the reactor, a flash tank connected with the cooler, a methylamine recovery system connected with the flash tank, a purification and refining system, the raw material storage tank system comprises a methylamine storage tank, a sodium isethionate solution storage tank and a catalyst storage container, the methylamine storage tank is provided with methylamine, the sodium isethionate solution storage tank is provided with a sodium isethionate solution, and the catalyst storage tank is provided with a Zr-modified HZSM-5 catalyst.
2. The production system of sodium methyl taurate according to claim 1, characterized by: The reactor is a high-pressure reaction kettle which is provided with a magnetic drive stirrer, and the cooler is a tube heat exchanger.
3. The production system of sodium methyl taurate according to claim 1, characterized by: A feeding pipeline one is arranged between the sodium isethionate solution storage tank and the reactor, the methylamine storage tank is a pressure storage tank, a feeding pipeline two is arranged between the methylamine storage tank and the reactor, and the feeding pipeline one and the feeding pipeline two are both provided with a high-pressure plunger pump.
4. The production system of sodium methyl taurate according to claim 1, characterized by: The flash tank comprises a vertical tank body.
5. The system for producing sodium methyl taurate according to claim 1, wherein: The methylamine recovery system comprises a compressor, a methylamine condenser and a methylamine temporary storage tank which is connected with the methylamine storage tank through a pipeline.
6. The production system of sodium methyl taurate according to claim 1, characterized by: The purification and refining system comprises a decoloring tank which is provided with a stirrer and a heating jacket and is filled with activated carbon.
7. The system for producing sodium methyl taurate according to claim 1, wherein: The purification and refining system further comprises a filtering device, an evaporation and concentration device, a crystallization tank, a solid-liquid separation device and a drying device.
8. The system for producing sodium methyl taurate according to claim 7, wherein: The evaporation and concentration device is a vacuum evaporator, and the solid-liquid separation device is a centrifuge.
9. The production system of sodium methyl taurate according to claim 1, characterized by: The Zr-modified HZSM-5 catalyst is prepared by the following method: TEOS, TPAOH, aluminum isopropoxide, deionized water, PEG and Zr(NO3)4 5H2O are weighed according to the molar ratio of SiO2:Al2O3:TPAOH:H2O:PEG:Zr(NO3)4 5H2O=1:0.01:0.3:50:0.01:0.01, and are uniformly stirred at 60 DEG C to obtain a xerogel, the temperature is lowered to 15-25 DEG C, and the xerogel is placed for 24 hours, the xerogel is baked in a sealed container in a water vapor environment at 155-160 DEG C for 27 hours, is washed with water until neutral, is dried at 100 DEG C, is dissolved in a TPAOH / NaOH solution and recrystallized, is washed with water until neutral, is dried at 100 DEG C for 8 hours, is calcined at 550 DEG C for 6 hours, is cooled, is treated with a 1.5 mol / L ammonium chloride solution in an ion exchange process at 60 DEG C, and is dried to obtain the Zr-modified HZSM-5 catalyst.