CN112479906B - Production process of meglumine - Google Patents
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- CN112479906B CN112479906B CN202011452435.1A CN202011452435A CN112479906B CN 112479906 B CN112479906 B CN 112479906B CN 202011452435 A CN202011452435 A CN 202011452435A CN 112479906 B CN112479906 B CN 112479906B
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C213/00—Preparation of compounds containing amino and hydroxy, amino and etherified hydroxy or amino and esterified hydroxy groups bound to the same carbon skeleton
- C07C213/02—Preparation of compounds containing amino and hydroxy, amino and etherified hydroxy or amino and esterified hydroxy groups bound to the same carbon skeleton by reactions involving the formation of amino groups from compounds containing hydroxy groups or etherified or esterified hydroxy groups
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- B—PERFORMING OPERATIONS; TRANSPORTING
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- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
- B01J23/89—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals
- B01J23/8933—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals also combined with metals, or metal oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
- B01J23/8993—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals also combined with metals, or metal oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with chromium, molybdenum or tungsten
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
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Abstract
The application relates to a production process of meglumine, which comprises the following steps: s1: condensing monomethylamine with glucose in absolute ethyl alcohol to obtain a polyporus salt; s2: adding a catalyst and absolute ethyl alcohol into the Schiff's salt, introducing hydrogen to react to obtain hydride, crystallizing to obtain solid hydride, adding water to melt the hydride, adding disodium ethylene diamine tetraacetate, concentrating under reduced pressure, performing spin filtration to obtain a meglumine crude product, and purifying the meglumine crude product; the catalyst is skeleton nickel, and the preparation steps of the skeleton nickel are as follows: stirring liquid alkali, heating to 40-47 deg.C, gradually adding aluminum-nickel-chromium-rhodium alloy powder, naturally heating to 85-100 deg.C, maintaining at the temperature for 2.5-3 hr, cooling to 55-65 deg.C, stopping stirring, and washing with water and anhydrous ethanol. The application has the effect of improving the production efficiency of meglumine.
Description
Technical Field
The application relates to the field of production of meglumine, in particular to a production process of meglumine.
Background
Meglumine, also called glucamine or 1-deoxy-1-methylamine sorbitol, is used for preparing contrast agents, such as diatrizoate and meglumine cholate, and also used as an auxiliary material or an intermediate of other medicines.
In the related technology, glucose is firstly condensed with methylamine in absolute ethyl alcohol to form a sodium benzoate, hydrogen is taken as a hydrogen source, raney nickel is taken as a catalyst to synthesize meglumine, and the catalyst is hydrogenated to obtain the sodium benzoate.
The reaction is slow, and the production efficiency is low.
Disclosure of Invention
In order to improve the production efficiency of meglumine, the application provides a production process of meglumine.
The production process of meglumine adopts the following technical scheme:
a production process of meglumine comprises the following steps:
s1: condensing monomethylamine with glucose in absolute ethyl alcohol to obtain a Schiff's salt;
s2: adding a catalyst and absolute ethyl alcohol into the Schiff's salt, introducing hydrogen to react to obtain hydride, crystallizing to obtain solid hydride, separating out the catalyst in the solid hydride to obtain a meglumine crude product, and purifying the meglumine crude product;
the catalyst is skeleton nickel, and the preparation steps of the skeleton nickel are as follows: stirring liquid caustic soda, heating to 40-47 deg.C, gradually adding aluminum-nickel-chromium-rhodium alloy powder, naturally heating to 85-100 deg.C, maintaining at the temperature for 2.5-3 hr, cooling to 55-65 deg.C, stopping stirring, repeatedly washing with water until pH is 7, washing with anhydrous ethanol until ethanol content is not less than 95%, and discharging.
By adopting the technical scheme, aluminum is dissolved in the alkali liquor to obtain the nickel framework modified by chromium and rhodium, the catalysis efficiency of the nickel framework on the hydrogenation of the Schiff's salt is higher, and the production efficiency and the conversion rate of the meglumine are improved.
Optionally, in the aluminum nickel chromium rhodium alloy, by weight, 32-58% of aluminum, 38-48% of nickel, 2-7% of chromium, 6-10% of rhodium and 80-100 meshes of aluminum nickel chromium rhodium alloy are adopted.
By adopting the technical scheme, the alkali liquor reacts with aluminum in the aluminum-nickel-chromium-rhodium alloy in the proportion to obtain a nickel skeleton modified by chromium and rhodium with a certain content, and the nickel skeleton has higher catalytic efficiency on hydrogenation of the sodium benzoate, thereby being beneficial to improving the production efficiency of meglumine.
Optionally, the liquid alkali is 23-28wt% of sodium hydroxide, and the mass ratio of the aluminum-nickel-chromium-rhodium alloy to the alkali liquor is 1: (4.5-5.5).
Optionally, in step S1, monomethylamine gas is dissolved in absolute ethanol at a temperature of 25 to 45 ℃ to prepare monomethylamine absolute ethanol solution, glucose is added while stirring, and after the addition, the temperature is raised, and the temperature is controlled to 45 to 50 ℃ to dissolve the glucose, so as to obtain the salt of schiff.
Through adopting above-mentioned technical scheme, monomethylamine is at first dissolved in absolute ethyl alcohol solution, then make nongaseous glucose and the monomethylamine reaction of dissolving in absolute ethyl alcohol, make glucose can disperse evenly in ethanol solution through the stirring, monomethylamine can evenly distributed in absolute ethyl alcohol, thereby make glucose and monomethylamine can more even contact, the reaction is comparatively quick, and monomethylamine dissolves in ethanol earlier, the entering of control gas need not be in the reaction sequence, the reaction sequence is convenient for control.
Optionally, in step S1, monomethylamine gas is introduced into absolute ethanol while maintaining a pressure of 0.05 to 0.3 MPa.
By adopting the technical scheme, under the pressure, the absolute ethyl alcohol can maintain absorption of the monomethylamine, the rate of absorption of the monomethylamine is controlled to be stable and not too fast, the monomethylamine is relatively uniform and stable after being dissolved in the sewage ethyl alcohol, and the absolute ethyl alcohol can stably absorb the monomethylamine and has a fast absorption speed;
meanwhile, the pressure of the introduced hydrogen is relatively low, the requirement on equipment is low, the reaction is mild, and the safety is high.
Optionally, in step S1, the weight ratio of glucose, absolute ethyl alcohol, and monomethylamine is 1: (3-3.5): (0.3-0.4).
By adopting the technical scheme, the monomethylamine is excessive in proportion, the reaction rate of obtaining the Schiff's salt is high, the production efficiency is high, and the glucose can fully react.
Optionally, in step S2, the salt of schiff S, the catalyst and the absolute ethanol are added into a reaction vessel, air is removed, the reaction vessel is stirred and heated, hydrogen is introduced when the temperature reaches 43 to 47 ℃, the temperature is controlled to be 45 to 80 ℃, the pressure of the introduced hydrogen is 0.3 to 0.34Mpa, hydrogen is not absorbed any more, the residual hydrogen in the reaction vessel is removed, and the hydride is obtained by crystallization.
By adopting the technical scheme, under the pressure and the temperature of hydrogen introduction, the reaction rate between the Schiff's salt and the hydrogen is higher.
Optionally, in step S2, after dissolving the hydride in water, standing for 70-80h, taking out the liquid, adding disodium edetate, heating to 50-60 ℃, keeping the temperature for 0.75-1 h, concentrating under reduced pressure with a vacuum degree of 0.06-0.08Mpa until the hydride is viscous jelly, adding methanol, fully stirring, cooling to 1-5 ℃ for crystallization, and performing spin filtration and washing to obtain a meglumine crude product.
By adopting the technical scheme, after the hydride is dissolved in water, because the catalyst is solid, when the liquid is taken out, the catalyst is simultaneously separated, the separation of the catalyst is completed, and then the catalyst is recovered; the complexometry of the disodium ethylene diamine tetraacetate and the impurity metal ions such as nickel ions reduces the influence of the nickel ions on the meglumine, so that the meglumine is more stable.
Optionally, the air is driven off using the following steps: introducing nitrogen gas, removing the air in the kettle by 0.08-0.12, 0.12-0.17 and 0.18-0.22Mpa respectively, and introducing hydrogen gas by 0.08-0.12, 0.12-0.17 and 0.18-0.22Mpa respectively.
Through adopting above-mentioned technical scheme, driving away the air with nitrogen gas earlier, nitrogen gas is driven away to reuse hydrogen for the air is driven away cleaner, has improved the effect of driving away of air, makes hydrogenation process go on more smoothly.
Optionally, in step S2, the mass ratio of the salt, the catalyst, the hydrogen gas, the absolute ethyl alcohol, and the water is 1: (0.007-0.013): (0.07-0.08): (0.01-0.03): (0.5-0.6): (0.001-0.003).
By adopting the technical scheme, under the condition of the proportion of the raw materials, the sculller salt has a faster hydrogenation rate, the meglumine has a higher yield, and the yield can reach 87-97%.
In summary, the present application includes at least one of the following beneficial technical effects:
the nickel skeleton modified by chromium and rhodium has higher catalytic efficiency on hydrogenation of the Schiff salt, and the production efficiency of the meglumine is improved; and the production efficiency of the meglumine is further improved by setting the proportion and the conditions of the raw materials in the reaction, and the conversion rate is favorably improved.
Detailed Description
The present application is described in further detail in conjunction with the following.
Glucose, pharmaceutical grade, the manufacturer is Xian Tianzheng pharmaceutic adjuvant, inc.;
monomethylamine (CH) 3 NH 2 ) The manufacturer is Zhengzhou Xingzao chemical technology limited company;
absolute ethyl alcohol, pharmaceutical grade, model YF-841, brand Kangyuan, purchased from Yongfa City trade Co., ltd;
disodium ethylene diamine tetraacetate, pharmaceutical grade, is from Shanxi Zhengyi pharmaceutical adjuvant Co., ltd;
methanol, pharmaceutical grade, available from henan hui resins ltd.
Preparation example 1
The preparation method of the skeleton nickel comprises the following steps:
the aluminum-nickel-chromium-rhodium alloy comprises, by weight, 39% of aluminum, 48% of nickel, 7% of chromium and 6% of rhodium, and the aluminum-nickel-chromium-rhodium alloy is 80-100 meshes.
The preparation method of the aluminum-nickel-chromium-rhodium alloy comprises the steps of melting aluminum at 800 ℃, melting rhodium, nickel and chromium at 2500 ℃, adding the molten rhodium, nickel and chromium into the molten aluminum, uniformly stirring, cooling, melting the alloy by adopting a spraying method, spraying and quenching to obtain the aluminum-nickel-chromium-rhodium alloy.
Stirring a 23wt% sodium hydroxide solution, heating to 47 ℃, and gradually adding aluminum nickel chromium rhodium alloy powder, wherein the mass ratio of the aluminum nickel chromium rhodium alloy to the alkali liquor is 1: and 4.5, naturally heating to 100 ℃, keeping the temperature for 2.5 hours, cooling to 65 ℃, stopping stirring, repeatedly washing with water until the pH is 7, then washing with absolute ethyl alcohol until the content of the ethyl alcohol in the feed liquid is 95%, and discharging.
Preparation example 2
The difference from preparation example 1 is that: the aluminum-nickel-chromium-rhodium alloy comprises, by weight, 50% of aluminum, 40% of nickel, 3% of chromium and 7% of rhodium.
Stirring 25wt% of sodium hydroxide solution, heating to 43 ℃, and gradually adding aluminum nickel chromium rhodium alloy powder, wherein the mass ratio of the aluminum nickel chromium rhodium alloy to the alkali liquor is 1: and 5, naturally heating to 90 ℃, keeping the temperature for 2.6 hours, cooling to 60 ℃, stopping stirring, repeatedly washing with water until the pH is 7, washing with absolute ethyl alcohol until the content of the ethyl alcohol in the feed liquid is 96%, and discharging.
Preparation example 3
The difference from preparation example 1 is that:
the difference from preparation example 1 is that: the aluminum-nickel-chromium-rhodium alloy comprises, by weight, 52% of aluminum, 38% of nickel, 2% of chromium and 8% of rhodium.
Stirring a 28wt% sodium hydroxide solution, heating to 40 ℃, and gradually adding aluminum nickel chromium rhodium alloy powder, wherein the mass ratio of the aluminum nickel chromium rhodium alloy to the alkali liquor is 1:5.5, naturally heating to 85 ℃, keeping the temperature for 3 hours, cooling to 55 ℃, stopping stirring, repeatedly washing with water until the pH is 7, then washing with absolute ethyl alcohol until the content of the ethyl alcohol in the feed liquid is 98%, and discharging.
Example 1
A production process of meglumine comprises the following steps:
s1: introducing monomethylamine gas into absolute ethyl alcohol at 25 ℃ and under the pressure of 0.3MPa to prepare monomethylamine absolute ethyl alcohol solution, and then adding 110Kg of glucose while stirring, wherein the weight ratio of the glucose to the absolute ethyl alcohol to the monomethylamine is 1:3:0.4, heating after adding, and controlling the temperature to be 45 ℃ to dissolve the glucose to obtain the salt of the Schiff's family;
s2: adding a catalyst (the catalyst is the skeletal nickel obtained in the preparation example 1) and absolute ethyl alcohol into a Schiff's salt, removing air, stirring and heating, introducing hydrogen when the temperature reaches 47 ℃, controlling the temperature at 80 ℃, introducing the hydrogen under the pressure of 0.3Mpa until the hydrogen is not absorbed any more, removing residual hydrogen in a kettle, crystallizing to obtain a solid hydride, adding water to melt the hydride, standing for 80 hours, adding disodium ethylenediamine tetraacetic acid, heating to 50 ℃, preserving the temperature for 1 hour, performing suction filtration on liquid by using a sand rod, performing reduced pressure concentration on the liquid under the vacuum condition of 0.06Mpa until the liquid is viscous jelly, adding methanol, stirring, cooling and crystallizing at 7 ℃, performing spin filtration and washing to obtain a meglumine crude product, and purifying the meglumine crude product. In the step, the mass ratio of the salt, the catalyst, the hydrogen, the absolute ethyl alcohol and the water is 1:0.007:0.08:0.01:0.6, the mass ratio of the solid hydride to the ethylene diamine tetraacetic acid and the methanol is 1:0.0033:0.36.
the air removal process comprises the following steps: introducing nitrogen gas to remove the air in the kettle at 0.12, 0.12 and 0.22Mpa respectively, and introducing hydrogen gas to remove the nitrogen gas in the kettle at 0.08, 0.17 and 0.18Mpa respectively after removing.
Example 2
A production process of meglumine comprises the following steps:
s1: introducing monomethylamine gas into absolute ethyl alcohol at 40 ℃ and under the pressure of 0.25MPa to prepare monomethylamine absolute ethyl alcohol liquid, and then adding 110Kg of glucose while stirring, wherein the weight ratio of the glucose to the absolute ethyl alcohol to the monomethylamine is 1:3.27:0.38, heating after adding, and controlling the temperature to 47 ℃ to dissolve glucose to obtain the salt of the Schiff's family;
s2: adding a catalyst (the catalyst is the skeletal nickel obtained in the preparation example 1) and absolute ethyl alcohol into a polyporus salt, removing air, stirring and heating, introducing hydrogen when the temperature reaches 45 ℃, controlling the temperature at 55 ℃, introducing the hydrogen under the pressure of 0.32Mpa until hydrogen is not absorbed any more, removing residual hydrogen in a kettle, crystallizing to obtain a solid hydride, adding water to melt the hydride, standing for 73 hours, adding disodium ethylenediamine tetraacetate, heating to 55 ℃, keeping the temperature for 0.85 hours, performing suction filtration on liquid by using a sand rod, performing reduced pressure concentration on the liquid under the condition of 0.07Mpa until the liquid is viscous jelly, adding methanol, stirring, performing cooling crystallization at 4 ℃, performing spin filtration and washing to obtain a meglumine crude product, and purifying the meglumine crude product. In the step, the mass ratio of the sodium benzoate to the hydrogen to the absolute ethyl alcohol is 1:0.01:0.08:0.02:0.58, wherein the mass ratio of the solid hydride to the ethylene diamine tetraacetic acid and the methanol is 1:0.004:0.33.
the air removal process comprises the following steps: introducing nitrogen gas to remove the air in the kettle at 0.1, 0.15 and 0.2Mpa respectively, and introducing hydrogen gas to remove the nitrogen in the kettle at 0.1, 0.15 and 0.2Mpa respectively.
Example 3
A production process of meglumine comprises the following steps:
s1: introducing monomethylamine gas into absolute ethyl alcohol at 45 ℃ and under the pressure of 0.05MPa to prepare monomethylamine absolute ethyl alcohol solution, and then adding 110Kg of glucose while stirring, wherein the weight ratio of the glucose to the absolute ethyl alcohol to the monomethylamine is 1:3.5:0.3, heating up after the addition, and controlling the temperature to be 50 ℃ to dissolve the glucose to obtain the sodium benzoate;
s2: adding a catalyst (the catalyst is the skeletal nickel obtained in the preparation example 1) and absolute ethyl alcohol into a polyporus salt, removing air, stirring and heating, introducing hydrogen when the temperature reaches 43 ℃, controlling the temperature at 45 ℃, introducing the hydrogen under the pressure of 0.34Mpa until hydrogen is not absorbed any more, removing residual hydrogen in a kettle, crystallizing to obtain a solid hydride, adding water to melt the hydride, standing for 70 hours, adding disodium ethylenediamine tetraacetate, heating to 60 ℃, keeping the temperature for 0.75 hours, then performing suction filtration on liquid by using a sand rod, performing reduced pressure concentration on the liquid under the vacuum condition of 0.08Mpa until the liquid is viscous jelly, adding methanol, stirring, performing cooling crystallization at the temperature of 2 ℃, performing spin filtration and washing to obtain a meglumine crude product, and purifying the meglumine crude product. In the step, the mass ratio of the sodium benzoate to the hydrogen to the anhydrous ethanol is 1:0.013:0.07:0.03:0.5, the mass ratio of the solid hydride to the ethylene diamine tetraacetic acid and the methanol is 1:0.0033:0.36.
the air removal process comprises the following steps: introducing nitrogen gas to remove the air in the kettle at 0.08, 0.17 and 0.18Mpa respectively, and introducing hydrogen gas to remove the nitrogen in the kettle at 0.12, 0.12 and 0.22Mpa respectively.
Example 4
The difference from example 2 is that: the catalyst was skeletal nickel prepared in preparation example 2.
Example 5
The difference from example 2 is that: the catalyst was skeletal nickel obtained in preparation example 3.
Example 6
The difference from example 4 is that:
and step S2, starting to introduce hydrogen when the temperature reaches 47 ℃, controlling the temperature at 80 ℃, introducing the hydrogen under the pressure of 0.3Mpa until the hydrogen is not absorbed any more, removing residual hydrogen in the kettle, and crystallizing to obtain the solid hydride.
Example 7
The difference from example 4 is that:
and step S2, starting to introduce hydrogen when the temperature reaches 43 ℃, controlling the temperature at 45 ℃, introducing the hydrogen at 0.34Mpa until the hydrogen is not absorbed any more, removing residual hydrogen in the kettle, and crystallizing to obtain the solid hydride.
Comparative example 1
The difference from example 4 is that:
the specific preparation steps of the skeleton nickel are as follows: the aluminum-nickel-chromium-rhodium alloy powder is replaced by aluminum-nickel alloy with equal weight fraction, wherein the aluminum content in the aluminum-nickel alloy is 53wt%, and the nickel content in the aluminum-nickel alloy is 47wt%.
Performance detection
The reaction principle is as follows:
the amount of the substance of meglumine finally obtained in examples 1 to 7 and comparative example 1 was measured, and the yield = amount of the substance of meglumine/amount of the substance of glucose 100% was calculated and recorded;
and adding a catalyst and absolute ethyl alcohol into the sculller salt, starting to introduce hydrogen, recording the time between the solid hydride obtained by the hydrogenation step and the time between the solid hydride and the reference example 1, calculating and recording the ratio of the time between the solid hydride and the reference example 1, wherein if the ratio is less than 1, the reaction rate/production efficiency is superior to that of the reference example 1, the smaller the ratio is, the higher the production efficiency is, and if the ratio is more than 1, the reaction rate/production efficiency is lower than that of the reference example 1.
The results are shown in Table 1.
TABLE 1 Performance test results
| Yield/%) | Ratio of | |
| Example 1 | 89.7 | 0.74 |
| Example 2 | 93.5 | 0.62 |
| Example 3 | 92.0 | 0.77 |
| Example 4 | 94.4 | 0.56 |
| Example 5 | 92.3 | 0.60 |
| Example 6 | 91.8 | 0.66 |
| Example 7 | 90.9 | 0.70 |
| Comparative example 1 | 78.2 | 1 |
As can be seen from Table 1, the ratios of examples 1 to 7 are all less than 1, and the production efficiencies of examples 1 to 7 are all higher than that of comparative example 1, so that the process conditions of the present application are better, and whether higher production efficiency can be achieved or not can be achieved. And from the yield, the application reaches 89.7-94.4%, which shows that the yield of the meglumine is greatly improved by creatively setting various conditions and the like in the production process.
In examples 1 to 3, the production process of example 2 was more excellent because the yield and production efficiency of example 2 were the highest.
In examples 2 and 4 to 5, the catalyst of preparation example 2 had higher catalytic efficiency because the yield was the highest and the production efficiency was the highest in example 4.
In examples 4 and 6 to 7, the yield and production efficiency of example 4 were superior to those of examples 6 to 7, so the hydrogenation conditions of example 4 were superior.
The above embodiments are preferred embodiments of the present application, and the protection scope of the present application is not limited by the above embodiments, so: all equivalent changes made according to the structure, shape and principle of the present application shall be covered by the protection scope of the present application.
Claims (9)
1. A production process of meglumine is characterized in that: the method comprises the following steps:
s1: condensing monomethylamine with glucose in absolute ethyl alcohol to obtain a Schiff's salt;
s2: adding a catalyst and absolute ethyl alcohol into the polyporus salt, introducing hydrogen to react to obtain hydride, crystallizing to obtain solid hydride, separating the catalyst in the solid hydride to obtain a meglumine crude product, and purifying the meglumine crude product;
the catalyst is skeleton nickel, and the preparation steps of the skeleton nickel are as follows: stirring liquid alkali, heating to 40-47 ℃, and then gradually adding aluminum-nickel-chromium-rhodium alloy powder, wherein the liquid alkali is 23-28wt% of sodium hydroxide, and the mass ratio of the aluminum-nickel-chromium-rhodium alloy to alkali liquor is 1: (4.5-5.5), wherein the aluminum nickel chromium rhodium alloy comprises, by weight, 32-58% of aluminum, 38-48% of nickel, 2-7% of chromium and 6-10% of rhodium; naturally heating to 85-100 deg.C, keeping the temperature for 2.5-3 hr, cooling to 55-65 deg.C, stopping stirring, washing with water repeatedly until pH is 7, washing with anhydrous ethanol until ethanol content is not less than 95%, and discharging.
2. The process for producing meglumine according to claim 1, wherein: the aluminum-nickel-chromium-rhodium alloy is 80-100 meshes.
3. The process for producing meglumine according to claim 1, wherein: in the step S1, monomethylamine gas is dissolved in absolute ethyl alcohol at the temperature of 25-45 ℃ to prepare monomethylamine absolute ethyl alcohol liquid, glucose is added while stirring, the temperature is raised after adding, and the temperature is controlled to be 45-50 ℃ to dissolve the glucose, so that the ceflower salt is obtained.
4. A process for the production of meglumine according to claim 3, wherein: in step S1, monomethylamine gas is introduced into absolute ethyl alcohol under the pressure of 0.05-0.3 MPa.
5. A process for the production of meglumine according to claim 3, wherein: in the step S1, the weight ratio of glucose, absolute ethyl alcohol and monomethylamine is 1: (3-3.5): (0.3-0.4).
6. The process for producing meglumine according to claim 1, wherein: and step S2, putting the Schiff' S salt, the catalyst and the absolute ethyl alcohol into a reaction container, removing air, stirring and heating, introducing hydrogen when the temperature reaches 43-47 ℃, controlling the temperature at 45-80 ℃ and the pressure at 0.3-0.34Mpa until hydrogen is not absorbed any more, removing residual hydrogen in the kettle, and crystallizing to obtain the hydride.
7. The process for producing meglumine according to claim 6, wherein: in the step S2, hydride is dissolved in water, standing is carried out for 70-80h, liquid is taken out, ethylene diamine tetraacetic acid disodium is added, heating is carried out at 50-60 ℃, heat preservation is carried out for 0.75-1 h, reduced pressure concentration is carried out, vacuum degree is 0.06-0.08Mpa, methanol is added when the liquid is viscous jelly, full stirring is carried out, cooling crystallization is carried out at 1-5 ℃, and a meglumine crude product is obtained after filtration and washing.
8. The process for producing meglumine according to claim 6, wherein: the air removal method comprises the following steps: introducing nitrogen gas, removing the air in the kettle by 0.08-0.12, 0.12-0.17 and 0.18-0.22Mpa respectively, and introducing hydrogen gas by 0.08-0.12, 0.12-0.17 and 0.18-0.22Mpa respectively.
9. The process of claim 6, wherein the reaction is carried out in the presence of a solvent selected from the group consisting of: in the step S2, the mass ratio of the salt, the catalyst, the hydrogen, the absolute ethyl alcohol and the water is 1: (0.007-0.013): (0.07-0.08): (0.01-0.03): (0.5-0.6): (0.001-0.003).
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