JPH07118213A - Production of alkanolamine - Google Patents

Abstract

PURPOSE:To provide a alkanolamine-production process capable of increasing the production ratio of a monoalkanolamine by the use of ammonia in the minimum required amount and obtaining on an industrial scale at an extremely economical cost. CONSTITUTION:In the reaction of ammonia with an alkylene oxide in the presence of a carbonate of ammonia and water, ammonia is used in the range of >1 mole and <=3.6 mole based on 1 mole of the alkylene oxide and 1 or more than one mole based on 1 mole of carbon dioxide contained in the carbonate of ammonia.

Description

Detailed Description of the Invention

[0001]

The present invention relates to ethanolamines,
The present invention relates to a method for producing alkanolamines such as isopropanolamines, and more particularly to a method for producing monoalkanolamines among these alkanolamines.

[0002]

2. Description of the Related Art Alkanolamines are easily obtained by reacting alkylene oxide with aqueous ammonia, and are industrially produced by this method. However, the alkanolamines obtained by this reaction are a mixture of monoalkanolamines, dialkanolamines and trialkanolamines, and controlling the production ratio thereof was an important issue.

Generally, as a method of increasing the production ratio of monoalkanolamine, for example, the reaction of ethylene oxide and ammonia is known as follows. That is, the reactivity of ethylene oxide with ammonia is slower than the reactivity of ethylene oxide with monoethanolamine or diethanolamine, and therefore the ratio of the reaction product changes depending on the ratio of ammonia to ethylene oxide, resulting in a large excess of ammonia. The production rate of monoethanolamine increases with increasing use (K. Weissermel, HJ Arpe, translated by Mitsuaki Mukaiyama, "Industrial Organic Chemistry-Main Raw Materials and Intermediates-" Tokyo Kagaku Dojin, P149, (1978)).

However, although the production ratio of monoalkanolamine can be increased by using ammonia water and increasing the molar ratio of ammonia / alkylene oxide, the volumetric efficiency of the reactor is deteriorated and excess ammonia water is removed. Since it is necessary to collect and recycle, there are problems that the energy consumption rate deteriorates, and the loads on the ammonia recovery system and the water recovery system increase.

In order to solve such a problem, there is a method of reducing the water content of ammonia as much as possible, but since water acts as a catalyst in this reaction, the activity decreases as it is. Therefore, as a countermeasure, use of a solid acid catalyst or a method of increasing the reaction temperature (see, for example, JP-A-49-47728, Zh.P.
rikl.Khim., 56, 1966 (1983), USP 4438281) and a method of reacting in a supercritical state (JP-A-59-13751, JP-A-59-3324).
7) has also been proposed, but problems such as the need for a high-pressure reactor and the increased load on the ammonia recovery system have not been solved because the reaction pressure becomes high.

[0006]

DISCLOSURE OF INVENTION Problems to be Solved by the Invention The inventors of the present invention firstly react ammonia with alkylene oxide to produce alkanolamines, and by carrying out the reaction in the presence of carbonates of ammonia, It was confirmed and proposed that the production ratio of monoalkanolamine can be remarkably increased without using a large excess of ammonia with respect to oxide.

However, even in the method of carrying out the reaction in the presence of the carbonate of ammonia, since the excess amount of ammonia is still used with respect to the alkylene oxide, the energy unit for recovering and recycling the excess amount of ammonia is It is difficult to say that an economical and industrial manufacturing method for alkanolamines has been established because the deterioration and the load on the ammonia recovery system increase. An object of the present invention is to provide a method for reacting ammonia and alkylene oxide in the presence of carbonates of ammonia and water, which is an economical and industrial method for producing alkanolamines in which the amount of ammonia used is minimized. To establish.

[0008]

Means for Solving the Problems As a result of intensive studies to solve the above problems, the present inventors have found that when ammonia is used in an amount of 1 or less in terms of molar ratio to alkylene oxide, a by-product. It was revealed that the selectivity of alkanolamines to the alkylene oxide used as a raw material was significantly decreased because of the increase in the amount. On the other hand, it was found that even if the molar ratio of ammonia to alkylene oxide is made larger than 3.6, the production ratio of alkanolamines no longer changes, and further the selectivity of alkanolamines to alkylene oxide used as a raw material does not change. The present invention has been reached.

That is, in the present invention, when ammonia and alkylene oxide are reacted in the presence of carbonates of ammonia and water, ammonia is used in the range of more than 1 and not more than 3.6 mol per mol of alkylene oxide. In addition, the method for producing alkanolamines is characterized by reacting 1 mol or more of ammonia with 1 mol of carbon dioxide contained in carbonates of ammonia. Hereinafter, the present invention will be described in more detail.

The alkanolamines referred to in the present invention are a general term for monoalkanolamines, dialkanolamines and trialkanolamines. For example, when ethylene oxide is used as a raw material, it means monoethanolamine, diethanolamine and triethanolamine, and when propylene oxide is used as a raw material, it means monoisopropanolamine, diisopropanolamine and triisopropanolamine.

In the method of the present invention, it is very important to select the amount of ammonia used within a limited specific range. The amount of ammonia used here means the sum of the amount of ammonia contained in the carbonates of ammonia used and the amount of ammonia supplied to the reaction system as ammonia. When the amount of ammonia used is less than this range, for example, when ethylene oxide is used as the alkylene oxide, the amount of by-produced monoethylene glycol and tetrahydroxyethylammonium hydroxide is significantly increased. Therefore, the selectivity of the alkanolamines with respect to the alkylene oxide used as the raw material is significantly reduced. Further, among the produced alkanolamines, the production ratio of monoalkanolamines decreases and the production ratio of trialkanolamines increases.

On the other hand, even if the amount of ammonia used is more than this range, the by-produced amounts of monoethylene glycol and tetrahydroxyethylammonium hydroxide do not change as compared with the case where the amount of ammonia within the range of the present invention is used. Therefore, the selectivity of the alkanolamines with respect to the alkylene oxide used as the raw material does not change. Further, the production ratio of mono-, di-, and trialkanolamines among the produced alkanolamines does not change. Therefore, even if the amount of ammonia used is made larger than this range, there is no advantage, and in addition, the ammonia used in excess is recovered and the energy for recycling to the reaction system is lost. Therefore, by selecting the amount of ammonia used within the specific range in the method of the present invention, an economical and industrial method for producing alkanolamines can be obtained in which the amount of ammonia used is minimized. The preferred amount of ammonia used is more than 1 mol of ammonia per mol of alkylene oxide and 3.
It is in the range of 6 mol or less.

On the other hand, in the present invention, the production ratio of the alkanolamines is controlled by changing the amount of the ammonia carbonates used, but 1 mol or more of ammonia is added to 1 mol of carbon dioxide contained in the ammonia carbonates. It is necessary to carry out the reaction with. The molar ratio of ammonia to alkylene oxide exceeds 1 mol and is 3.6
Even if the reaction is carried out within the following range, the reaction becomes very slow unless the reaction is carried out under the condition that the molar ratio of ammonia to carbon dioxide is 1 or more. Therefore, the preferred amount of ammonia used in the present invention is such that ammonia is used in the range of more than 1 mol and not more than 3.6 mol per mol of alkylene oxide, and to 1 mol of carbon dioxide contained in the carbonate of ammonia. It is a range that satisfies the condition of using 1 mol or more of ammonia.

In the method of the present invention, when the ammonia and the alkylene oxide are reacted with each other, the reaction is carried out in the presence of carbonates of ammonia, so that it is not necessary to use a large excess of ammonia as is conventionally known. It is possible to increase the production ratio of alkanolamines.

Ammonia carbonates used in the method of the present invention include ammonium carbonate, ammonium bicarbonate,
In addition to compounds such as ammonium carbamate, the following can also be used: For example, carbon dioxide may be mixed with ammonia water at an arbitrary ratio to form ammonia carbonates. The carbon dioxide used in this case may be dry ice, liquid carbon dioxide, carbonated water in which carbon dioxide is dissolved in water, or gaseous carbon dioxide.

[0016] The ammonia water referred to here is, in addition to normal ammonia water in which ammonia is dissolved in water,
It means either water and liquid ammonia or a mixture of gaseous ammonia. As a method for mixing ammonia and carbon dioxide, alkylene oxide may be introduced into the reactor after mixing ammonia and carbon dioxide, or carbon dioxide may be introduced into the reactor in which ammonia and alkylene oxide exist. However, ammonia may be introduced into the reactor where alkylene oxide and carbon dioxide are present, or ammonia and carbon dioxide may be introduced separately into the reactor where alkylene oxide is present, or alkylene oxide may be introduced into the reactor. Ammonia and carbon dioxide may be introduced separately.

Further, a substance which releases carbon dioxide under the reaction conditions to form ammonia and a salt can be used. As such an example, there are, for example, those obtained by absorbing carbon dioxide in an anion exchange resin, and those obtained by absorbing carbon dioxide in a solvent which easily absorbs carbon dioxide such as ethylene carbonate.

The amount of these carbonates of ammonia used is such that the number of moles of carbon dioxide contained in the carbonates of ammonia is from 0.05 to 1 mole of alkylene oxide.
It is in the range of 3 moles. Within this range, the larger the amount of ammonia carbonates used, the larger the production ratio of monoalkanolamine, and accordingly the production ratio of dialkanolamine and trialkanolamine can be suppressed. Therefore, the production ratio of monoalkanolamine can be arbitrarily controlled by controlling the amount of the carbonates of ammonia used. If the amount of ammonia carbonate used is less than this range, the effect of increasing the production ratio of monoalkanolamine is small, and if it is more than this range, the effect is sufficient, but it is not preferable in consideration of economic efficiency.

In the method of the present invention, when the ammonia and the alkylene oxide are reacted in the presence of the carbonate of ammonia, the reaction is performed in the presence of water. Water acts as a catalyst for the reaction between ammonia and alkylene oxide, enhances the reaction activity, and has the effect of lowering the reaction pressure because it dissolves ammonia and carbon dioxide. The amount of water used is in the range of 1 to 20 mol per mol of alkylene oxide. If the amount of water used is less than this range, the reaction rate will decrease, and if it is more than this range, the volumetric efficiency of the reactor will deteriorate.In addition, after the reaction, the energy consumption rate for separating and recovering water will deteriorate, This is not preferable because the load on the recovery system increases.

Examples of alkylene oxides used in the method of the present invention include ethylene oxide, propylene oxide, epichlorohydrin, glycidol, 1,2-epoxybutane, trans-2,3-epoxybutane, isobutylene oxide, cyclohexene oxide, styrene oxide. Etc. can be illustrated. Among these alkylene oxides, ethylene oxide, propylene oxide and the like are preferable.

In the method of the present invention, the reaction is usually carried out without a solvent, but any solvent which does not adversely influence the reaction can be used. Examples of these solvents include saturated hydrocarbons such as heptane, aromatic hydrocarbons such as toluene, N-methylpyrrolidin-2-one, N, N-dimethylacetamide, N-substituted such as hexamethylphosphoric triamide. Amides, N,
N-diethylaniline, N-methylmorpholine, pyridine,
Tertiary amines such as triethanolamine, sulfones such as sulfolane, sulfoxides such as dimethyl sulfoxide, urea derivatives such as 1,3-dimethyl-2imidazolidinone, carbonates such as ethylene carbonate, and tributylphosphine. Examples thereof include phosphine oxides such as oxides.

The reaction temperature in the method of the present invention is 20 to 80 ° C.
Is preferred. If the reaction temperature is low, the reaction rate will be low, and if it is high, the reaction pressure will be high, which is not preferable. The reaction pressure is determined by the autogenous pressure at a predetermined reaction temperature, and this pressure may be maintained. Usually, it is 1 to 50 kg / cm ² (gauge pressure).

The reaction time in the method of the present invention varies depending on the amount of ammonia carbonate used, the amount of ammonia used, the amount of alkylene oxide used, the amount of water used, the reaction temperature, etc., but it is usually 5 minutes to 10 hours, preferably 10 minutes ~
5 hours.

The method of the present invention can be carried out by any of a batch method, a semi-batch method and a continuous method. For example, as an example of the batch method, the reactor is charged with ammonia carbonates, ammonia, water, and optionally a solvent,
The reaction is carried out while supplying alkylene oxide at a constant rate with a pump. Further, in the case of the continuous method, ammonia carbonates, ammonia, water, alkylene oxide and, if necessary, a solvent are continuously supplied to one of the reactors, and the reaction mixture is continuously withdrawn from the other to carry out the reaction. Is done. At this time, as a method of adding the alkylene oxide, the alkylene oxide may be added all at once from the reactor inlet, or may be dividedly added from the intermediate portion from the inlet to the outlet of the reactor.

[0025]

EXAMPLES The present invention will now be described in more detail with reference to examples.

Example 1 Internal volume 1 equipped with a thermometer, a pressure gauge, a heating and stirring device and an inlet for ethylene oxide (hereinafter abbreviated as EO)
A liter stainless steel reactor was charged with 211.0 g (2.20 mol) of ammonium carbonate and 60.0 g of water as raw materials. After replacing the inside of the reactor with nitrogen, 467 g of 40.7% ammonia water was added, and the temperature was raised to 40 ° C. before EO 19
4.0 g (4.40 mol) were introduced in 60 minutes. The conditions are ammonia / EO molar ratio 3.54, ammonia / carbon dioxide molar ratio 7.
09, carbon dioxide / EO molar ratio 0.50, water / EO molar ratio 4.74. During this period, the reaction temperature was maintained at 39-41 ° C and the pressure was 3.
It showed 4 to 4.1 kg / cm ² G. After EO supply is completed, 30 at 40 ℃
Aged for minutes.

After completion of the reaction, the reaction solution was analyzed by liquid chromatography to find that the conversion of EO was 99.99%, and 162.6 g (2.66) of monoethanolamine (hereinafter abbreviated as MEA).
mol), diethanolamine (hereinafter abbreviated as DEA) 53.2 g
(0.51 mol) and triethanolamine (hereinafter abbreviated as TEA) 34.0 g (0.23 mol) were produced. The production ratio of MEA, DEA and TEA was 65.1: 21.3: 13.7 by weight. In addition, ethylene glycol (hereinafter abbreviated as MEG)
1.12 g (0.018 mol), tetrahydroxyethyl ammonium hydroxide (abbreviated as quaternary salt below) 0.82 g
(0.0039 mol) and diethylene glycol amine (below
0.24g (0.0022mol) was a by-product.

Proportion of EO used as a raw material for MEA, DEA and TEA (hereinafter abbreviated as effective utilization rate of EO. Effective utilization rate (%) = (MEA mole + 2 × DEA mole + 3 × TEA mole) × 100 / EO mol) was 99.1%.

Example 2 In Example 1, the amount of water used was changed to 115.5 g, and 41.7%
The reaction was performed in the same manner as in Example 1 except that 366 g of aqueous ammonia was used. This condition corresponds to an ammonia / EO molar ratio of 3.04, an ammonia / carbon dioxide molar ratio of 6.08, a carbon dioxide / EO molar ratio of 0.50, and a water / EO molar ratio of 4.64. During this time, the reaction temperature was maintained at 39 to 41 ° C, and the pressure was 3.2 to 3.6 kg / cm ² G.

As a result, the conversion rate of EO was 100%, and the MEA
158.7g (2.60mol), DEA 52.8g (0.50mol) and TEA 37.4
g (0.25 mol) had formed. The production ratio of MEA, DEA and TEA was 63.8: 21.2: 15.0 by weight. Besides, ME
G 0.56g (0.0089mol), quaternary salt 1.26g (0.0060mol) and D
0.39 g (0.0060 mol) of GA was by-produced. The effective utilization rate of EO was 99.0%.

Example 3 In Example 1, the amount of water used was changed to 223.4 g, 40.3%
The reaction was performed in the same manner as in Example 1 except that 185 g of aqueous ammonia was used. This condition corresponds to an ammonia / EO molar ratio of 1.99, an ammonia / carbon dioxide molar ratio of 3.99, a carbon dioxide / EO molar ratio of 0.50, and a water / EO molar ratio of 4.71. During this time, the reaction temperature was maintained at 39 to 41 ° C., and the pressure was 1.7 to 2.4 kg / cm ² G.

As a result, the conversion rate of EO was 100%, and the MEA
142.2g (2.33mol), DEA 46.2g (0.44mol) and TEA 49.8
g (0.33 mol) had formed. The production ratio of MEA, DEA and TEA was 59.7: 19.4: 20.9 by weight. Besides, ME
G 3.08g (0.050mol), quaternary salt 4.89g (0.023mol) and DGA
0.64 g (0.0061 mol) was by-produced. Effective utilization of EO is 9
It was 6.5%.

Example 4 In Example 1, the amount of water used was changed to 277.6 g, 40.8%
The reaction was performed in the same manner as in Example 1 except that 95 g of aqueous ammonia was used. This condition corresponds to an ammonia / EO molar ratio of 1.52, an ammonia / carbon dioxide molar ratio of 3.04, a carbon dioxide / EO molar ratio of 0.50, and a water / EO molar ratio of 4.70. During this time, the reaction temperature was kept at 38 to 41 ° C., and the pressure was 1.5 to 2.7 kg / cm ² G.

As a result, the conversion rate of EO was 100%, and the MEA
134.3g (2.20mol), DEA 42.1g (0.40mol) and TEA 57.6
g (0.39 mol) had formed. The production ratio of MEA, DEA and TEA was 57.4: 18.0: 24.6 by weight. Besides, ME
G 5.51g (0.089mol), quaternary salt 9.72g (0.046mol) and DGA
0.50 g (0.0047 mol) was by-produced. Effective utilization of EO is 9
It was 3.7%.

Comparative Example 1 In Example 1, the amount of water used was changed to 330.9 g, and 15.7%
The reaction was performed in the same manner as in Example 1 except that 1 g of ammonia water was used and EO was supplied for 110 minutes. This condition is ammonia / EO molar ratio 1.00, ammonia / carbon dioxide molar ratio 2.0
0, carbon dioxide / EO molar ratio 0.50, water / EO molar ratio 4.69. During this time, the reaction temperature was maintained at 38-41 ° C and the pressure was 1.
It showed 4 to 4.0 kg / cm ² G.

As a result, the conversion rate of EO was 100%, and the MEA
102.8g (1.68mol), DEA 30.9g (0.29mol) and TEA 47.6
g (0.32 mol) had formed. The production ratio of MEA, DEA and TEA was 56.7: 17.0: 26.3 by weight. Besides, ME
G 27.5g (0.44mol), quaternary salt 31.0g (0.15mol) and DGA
0.54 g (0.0052 mol) was by-produced. Effective utilization of EO is 7
It was 3.6%.

According to Comparative Example 1, the ammonia / EO molar ratio was 1.
In the case of 00, it can be seen that MEG and quaternary salt are large by-products and the effective utilization rate of EO is significantly deteriorated.

Comparative Example 2 561 g of 40.0% ammonia water was used in Example 1,
The reaction was performed in the same manner as in Example 1 except that EO was supplied for 60 minutes. These conditions are: ammonia / EO molar ratio 4.00, ammonia / carbon dioxide molar ratio 8.00, carbon dioxide / EO molar ratio 0.5.
0, the water / EO molar ratio corresponds to 4.75. During this time, the reaction temperature was 3
The temperature was maintained at 8 to 41 ° C, and the pressure was 3.5 to 4.0 kg / cm ² G.

As a result, the conversion rate of EO was 100%, and the MEA
159.3g (2.61mol), DEA 51.5g (0.49mol) and TEA 38.2
g (0.26 mol) had formed. The production ratio of MEA, DEA and TEA was 64.0: 20.7: 15.3 by weight. Besides, ME
G 0.58g (0.0093mol), quaternary salt 1.19g (0.0056mol) and D
GA 0.41g (0.0039mol) was by-produced. The effective utilization rate of EO was 99.0%.

According to Comparative Example 2, the ammonia / EO molar ratio was
Even if the reaction is carried out under the conditions of 4.00, there is no difference in the reaction results as compared with Example 1, which indicates that there is no effect of using a large amount of ammonia.

Example 5 In Example 1, the amount of ammonium carbonate charged was 305.6 g.
(3.18 mol), the amount of water charged to 203 g, the amount of 40.1% ammonia water charged to 259 g, and the amount of EO charged to 155.0 g (3.52 mol) were changed to Example 1 except that EO was introduced in 90 minutes. The reaction was performed similarly. The conditions are: ammonia / EO molar ratio 3.54, ammonia / carbon dioxide molar ratio 3.93, carbon dioxide / EO molar ratio.
0.90, the water / EO molar ratio is 6.55. During this period, the reaction temperature was maintained at 36 to 40 ° C, and the pressure was 2.4 to 4.0 kg / cm ² G.
After the supply of EO was completed, aging was carried out at 40 ° C for 30 minutes.

After the completion of the reaction, the reaction solution was analyzed by liquid chromatography to find that the EO conversion was 100%.
5.4g (2.38mol), DEA 33.8g (0.32mol) and TEA 19.9g
(0.13 mol) had been produced. The production ratio of MEA, DEA and TEA was 73.0: 17.0: 10.0 by weight. Besides, ME
G 1.46g (0.024mol), quaternary salt 1.38g (0.0065mol) and
0.24 g (0.0022 mol) of DGA was produced as a by-product. The effective utilization rate of EO was 97.3%.

Comparative Example 3 The reaction was performed in the same manner as in Example 5 except that the amount of water charged was changed to 116.0 g and the amount of 40.0% ammonia water charged was changed to 402.7 g. This condition is that the ammonia / EO molar ratio is 4.5.
0, ammonia / carbon dioxide molar ratio 5.00, carbon dioxide / EO
The molar ratio is 0.90 and the water / EO molar ratio is 6.55. During this time, the reaction temperature was maintained at 38 to 40 ° C, and the pressure was 2.6 to 4.0 kg / cm ² G. After the supply of EO was completed, aging was carried out at 40 ° C for 30 minutes. After the reaction was completed, the reaction solution was analyzed by liquid chromatography to find that the EO conversion was 100%.
(2.40 mol), DEA 34.3 g (0.33 mol) and TEA 18.9 g (0.13
mol) had been produced. The production ratio of MEA, DEA and TEA was 73.4: 17.2: 9.4 by weight. Besides, MEG 1.49
g (0.024mol), quaternary salt 1.29g (0.0061mol) and DGA 0.
26 g (0.0022 mol) was by-produced. Effective utilization of EO is 9
It was 7.4%.

Example 6 In Example 1, the amount of ammonium carbonate charged was 131.0 g.
The reaction was carried out in the same manner as in Example 1 except that the amount of water charged to (1.36 mol) was changed to 0 g, the amount of 40.1% ammonia water charged to 480 g, and the amount of EO charged to 178.0 g (4.04 mol). This condition is ammonia / EO molar ratio 3.46, ammonia / carbon dioxide molar ratio
10.2, carbon dioxide / EO molar ratio 0.34, water / EO molar ratio 3.88
Equivalent to. During this time, keep the reaction temperature at 38-40 ° C and keep the pressure
It showed 2.9 to 4.0 kg / cm ² G.

After completion of the reaction, the reaction solution was analyzed by liquid chromatography to find that the EO conversion was 100%.
1.3g (1.99mol), DEA 59.6g (0.57mol) and TEA 40.1g
(0.27 mol) had been produced. The production ratio of MEA, DEA and TEA was 54.9: 27.0: 18.2 by weight. Besides, ME
G 0.84g (0.014mol), quaternary salt 0.89g (0.0042mol) and
0.31 g (0.0029 mol) of DGA was produced as a by-product. The effective utilization rate of EO was 97.5%.

Comparative Example 4 The reaction was carried out in the same manner as in Example 5, except that the amount of water charged was changed to 224.1 g and the amount of 40.0% ammonia water charged was changed to 55.9 g. This condition is ammonia / EO molar ratio of 1.0
0, ammonia / carbon dioxide molar ratio 2.94, carbon dioxide / EO
The molar ratio is 0.34 and the water / EO molar ratio is 3.88. During this time, the reaction temperature was maintained at 36 to 40 ° C, and the pressure was 2.5 to 4.0 kg / cm ² G. It took 110 minutes to supply EO.

After completion of the reaction, the reaction solution was analyzed by liquid chromatography to find that the EO conversion was 100%.
68.4g (1.12mol), DEA 36.3g (0.35mol) and TEA 52.6g
(0.35 mol) had been produced. The production ratio of MEA, DEA and TEA was 43.5: 23.1: 33.4 by weight. Besides, ME
G 30.4g (0.49mol), quaternary salt 35.4g (0.17mol) and DGA
0.61 g (0.0058 mol) was by-produced. The effective utilization rate of EO is
It was 71.3%.

[0048]

According to the method of the present invention, the production of alkanolamines having an increased production ratio of monoalkanolamines can be carried out economically and industrially extremely advantageously with the minimum required amount of ammonia used. Becomes

 ─────────────────────────────────────────────────── ─── Continuation of the front page (72) Inventor Kenji Suzuki 1-6 Takasago, Takaishi-shi, Osaka Mitsui Toatsu Chemical Co., Ltd.

Claims (2)

[Claims] 1. When reacting ammonia and alkylene oxide in the presence of ammonia carbonates and water, the amount of ammonia is 1 per mol of alkylene oxide.
Production of alkanolamines which is used in a range of more than 3.6 mol and less than 1 mol, and reacts with 1 mol or more of ammonia for 1 mol of carbon dioxide contained in the carbonates of ammonia. Method. 2. The production method according to claim 1, wherein the reaction temperature is 20 to 80 ° C.