CN106608834A - Method for cooperatively producing ethanolamine through liquid ammonia method and ammonium hydroxide method - Google Patents
Method for cooperatively producing ethanolamine through liquid ammonia method and ammonium hydroxide method Download PDFInfo
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- CN106608834A CN106608834A CN201510690201.3A CN201510690201A CN106608834A CN 106608834 A CN106608834 A CN 106608834A CN 201510690201 A CN201510690201 A CN 201510690201A CN 106608834 A CN106608834 A CN 106608834A
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Abstract
The invention relates to a method for cooperatively producing ethanolamine through a liquid ammonia method and an ammonium hydroxide method. The method comprises the steps that a raw material containing liquid ammonia and oxirane is sent into a liquid ammonia method reactor; after a reaction product is deaminized, mixed amine I is obtained, and recycled amine is circulated to the liquid ammonia method reactor; a raw material containing ammonium hydroxide and oxirane is introduced into an ammonium hydroxide method reactor; after a reaction product is deaminized and dehydrated, mixed amine II is obtained, and recycled amine returns to the ammonium hydroxide method reactor, wherein water circulates as a catalyst; and after being mixed, the mixed amine I and the mixed amine II are separated through a separation system comprising three or more rectifying towers, so that products, namely monoethanolamine (MEA), diethanolamine (DEA) and triethanolamine (TEA) are obtained. By means of the method, the problems that recycled amine carries water, so that activity of a liquid ammonia method catalyst is lowered, and even the liquid ammonia method catalyst is inactivated are solved; and the method can be applied to industrial production and transformation and expanding production of the ethanolamine.
Description
Technical field
The present invention relates to a kind of method of liquid ammonia process for caustic soda purification and Ammonia Process co-producing ethanol amine.Can be used for commercial production and the expansion of ethanolamine
In transforming.
Background technology
Ethanolamine is most important product in amido alcohol, is monoethanolamine (MEA), diethanolamine (DEA) and three ethanol
The general designation of amine (TEA), is water white transparency thick liquid under room temperature, have the property of amine and alcohol concurrently, of many uses, mainly
For aspects such as gas purifying agent, surfactant, pesticide, polyurethane and production ethyleneamineses, with boundless application
Prospect.The process route that industrial production ethanolamine is mainly reacted with excess ammonia using oxirane (EO).In water or alcohol
Under the catalysis of amine, 3 active hydrogens on amino molecule are replaced by ethyl successively, generate the mixture of MEA, DEA, TEA.
It is a traditional problem that EO ammonifications prepare ethanolamine, and domestic based on Ammonia Process research, catalysis liquid ammonia process for caustic soda purification is at home
Research is less.EO ammonifications are a strong exothermal reactions, and in ammonia-water systems, used as catalyst, ammonia concn more high energy consumption is more for water
It is low.Due to product separate on energy consumption it is higher, and products distribution have selectivity, so being faced with production very big
Competitive pressure.The research of catalysis liquid ammonia process for caustic soda purification is developed mainly for the catalyst of phase autoclave or supercritical reaction.No matter which
Technique is planted, less, energy consumption size is mainly reflected in product for the flow process and energy consumption difference of rectification under vacuum ethanolamine mixtures
In deamination dehydration.By contrast, as liquid ammonia process for caustic soda purification is not aqueous, it is not necessary to increase the energy consumption produced by dehydration, and product form
It is adjustable.Although catalysis liquid ammonia process for caustic soda purification have the advantages that it is very many, due to the critical temperature of liquefied ammonia it is relatively low, in the reaction such as
Fruit is not regulated and controled will be very high, so the low-temperature reactivity of catalyst becomes the problem stood in the breach.
Ethanolamine is heat-sensitive substance, coking of easily decomposing at high temperature, and side reaction occurs, and produces band color impurities, sternly
Ghost image rings product quality and purposes.Therefore select suitable operating pressure interval, it is ensured that relatively low bottom temperature, reduce full tower
Pressure drop separates most important to product purification.
CN101885686A discloses a kind of method for producing ethanolamine.Oxirane and liquefied ammonia are adopted for raw material, with ZSM-5
For catalyst, ammonia is 0.5～15 with the molar ratio of oxirane, and reaction temperature is 50～100 DEG C, and system pressure is
4～12MPa, liquid phase air speed is in 0.5～4h-1Under conditions of, reaction generates ethanolamine.Solve reaction temperature in prior art
Height, the high technical problem of system pressure.
CN101555208A discloses a kind of ammonia still process dewatering process of ethanolamine.Ethanolamine mixtures containing ammonia, water are sent
Enter the ethanolamine mixed liquor of ammonia still, overhead condensation liquid ammonia recovery, tower reactor water containing major part and a small amount of ammonia through flash tank, gas
Steam from flash drum overhead after change, ammonia tank is returned Jing after compressor, condenser are condensed into liquefied ammonia.Ethanolamine mixed liquor is entered
Dehydrating tower dehydration is recycled, and enters tail ammonia absorber spray-absorption from overhead condenser remaining ammonia out.The method can
Reclaim whole water and ammonia in ethanolamine production.
In method of the liquid ammonia process for caustic soda purification with Ammonia Process co-producing ethanol amine, the ammonia of ammonia still overhead extraction can carry a small amount of water secretly, affect
Liquid ammonia process for caustic soda purification reacts, therefore cannot be directly as the raw material of liquid ammonia process for caustic soda purification technique.The product Jing deamination of Ammonia Process is dehydrated by the present invention
The raw material of the ammonia that reclaims afterwards and water as Ammonia Process, raw material of the ammonia reclaimed after liquid ammonia process for caustic soda purification deamination as liquid ammonia process for caustic soda purification, targetedly
Solve the problems referred to above.
The content of the invention
The technical problem to be solved is that water entrainment impact liquid ammonia process for caustic soda purification reaction in ammonia is reclaimed present in joint production process
Problem, there is provided a kind of method of new liquid ammonia process for caustic soda purification and Ammonia Process co-producing ethanol amine.Ammonia Process is separated in rectification under vacuum with liquid ammonia process for caustic soda purification
The flow process and energy consumption difference of ethanolamine mixtures less, can share a set of distillation system, convenient to adjust load.Liquid ammonia process for caustic soda purification reacts
During do not need water, make recovery ammonia efficiency high, energy consumption is low.The ammonia that the product of Ammonia Process is reclaimed Jing after deamination dehydration
With water as Ammonia Process raw material, raw material of the ammonia reclaimed after liquid ammonia process for caustic soda purification deamination as liquid ammonia process for caustic soda purification reduce water to liquid ammonia process for caustic soda purification
Affect, can improve product quality, extend catalyst life, increase Business Economic Benefit.
To solve above-mentioned technical problem, technical scheme is as follows：A kind of side of liquid ammonia process for caustic soda purification and Ammonia Process co-producing ethanol amine
Method, comprises the following steps：
(1) raw material including liquefied ammonia and oxirane is passed through liquid ammonia process for caustic soda purification reactor and is reacted, and product is obtained Jing after deamination
To mixed amine I, ammonia return liquid ammonia process for caustic soda purification reactor cycles utilization；
(2) raw material including ammonia and oxirane is passed through Ammonia Process reactor and is reacted, and product deamination is dehydrated
To mixed amine II, ammonia and water return Ammonia Process reactor cycles utilization；
(3) refine from side line through monoethanolamine tower, diethanolamine tower, triethanolamine tower after mixing amine I and mixed amine II mixing
Product monoethanolamine (MEA), diethanolamine (DEA), triethanolamine (TEA) are obtained, tower top light component is back to previous respectively
Individual tower circulation is refined, and triethanolamine tower bottoms is used as triethanolamine certified products.
In above-mentioned technical proposal, it is preferred that liquid ammonia process for caustic soda purification reactor adopts shell and tube reactor, Ammonia Process reactor to adopt long tube
Formula reactor.
In above-mentioned technical proposal, it is preferred that the operating pressure of ammonia still is 1～5MPaA, and tower top temperature is 30～90 DEG C, is returned
Flow ratio is 0.1～10.It is furthermore preferred that the operating pressure of ammonia still is 1.3～3MpaA.
In above-mentioned technical proposal, it is preferred that the operating pressure of ammonia still is 1～5MPaA, and tower top temperature is 30～90 DEG C, is returned
Flow ratio is 0.1～10.It is furthermore preferred that the operating pressure of ammonia still is 1.3～3MpaA.
In above-mentioned technical proposal, it is preferred that the operating pressure of dehydrating tower is 0～200kPaA, and tower top temperature is 30～60 DEG C,
Reflux ratio is 1～10.It is furthermore preferred that the operating pressure of dehydrating tower is 50～150kPaA.
In above-mentioned technical proposal, it is preferred that the operating pressure of monoethanolamine tower is 0～30kPaA, and tower top temperature is 35～60 DEG C,
Reflux ratio is 10～100.It is furthermore preferred that the operating pressure of monoethanolamine tower is 0～10kPaA.
In above-mentioned technical proposal, it is preferred that diethanolamine tower operating pressure is 0～20kPaA, and tower top temperature is 50～150 DEG C,
Reflux ratio is 10～100.It is furthermore preferred that diethanolamine tower operating pressure is 0～5kPaA.
In above-mentioned technical proposal, it is preferred that triethanolamine tower operating pressure is 0～10kPa, and tower top temperature is 120-150 DEG C,
Reflux ratio is 10～100.It is furthermore preferred that triethanolamine tower operating pressure is 0～1kPaA.
In above-mentioned technical proposal, it is preferred that monoethanolamine tower, diethanolamine tower, triethanolamine column overhead light component are followed respectively
Ring is refined to the circulation of previous tower, and overhead condenser is located internally or externally with respect to rectifying column.
In above-mentioned technical proposal, it is preferred that ammonia still, ammonia still, dehydrating tower, monoethanolamine tower, diethanolamine tower, three
The tower reactor reboiler of ethanolamine tower is using the one kind in falling film evaporator, climbing film evaporator and luwa evaporator.
As the amine substances such as the product ethanolamine of liquid ammonia process for caustic soda purification and Ammonia Process, diethanolamine, triethanolamine belong to temperature-sensitive
Property material, can decompose coking when temperature is higher than 180 DEG C, contaminated equipment causes product yield to reduce, and affects technique
Economy.Therefore, product purification tower adopts negative-pressure operation, can select high efficiency packing and condenser is built-in reducing full tower pressure drop,
Tower reactor is kept to have certain light component to reduce bottom temperature, when tower reactor also can reduce the stop of tower bottoms by way of undergauge
Between.
Preferred technical scheme is：Tower bottom of rectifying tower reboiler is using in falling film evaporator, climbing film evaporator and luwa evaporator
One kind；Monoethanolamine column overhead light component is back to dehydrating tower, and diethanolamine column overhead light component is back to monoethanolamine tower,
Triethanolamine column overhead light component is back to diethanolamine tower；Rectifying column tower top condenser is preferably molded-in in rectifying column.
Using this kind of technical scheme, the technique that liquid ammonia process for caustic soda purification produces ethanolamine with Ammonia Process is combined, effectively reclaims ammonia and water,
And the ammonia for the product of Ammonia Process being reclaimed Jing after deamination dehydration respectively, used as the raw material of Ammonia Process, water is circulated as catalyst
Utilize, raw material of the ammonia reclaimed after liquid ammonia process for caustic soda purification deamination as liquid ammonia process for caustic soda purification, solve water entrainment in reclaiming ammonia and liquid ammonia process for caustic soda purification is reacted
Affect, refining spearation is circulated using tower top light component, using membrane evaporator, improve product yield, it is ensured that product matter
Amount, obtains preferable technique effect.
Description of the drawings
Fig. 1 is the process flow diagram of liquid ammonia process for caustic soda purification of the present invention and Ammonia Process co-producing ethanol amine.
In Fig. 1, R-101 is liquid ammonia process for caustic soda purification reactor, and R-102 Ammonia Process is reactor, and T101 is ammonia still, and T102 is ammonia
Recovery tower, T103 are dehydrating tower, and T104 is monoethanolamine tower, and T105 is diethanolamine tower, and T106 is triethanolamine tower,
E101 is monoethanolamine overhead condenser, and 1 is liquid ammonia process for caustic soda purification product, and 2 is that ammonia still T101 reclaims ammonia, and 3 is ammonia still process
Tower T101 tower bottoms, 4 is Ammonia Process product, and 5 is that recovery ammonia tower T102 reclaims ammonia, and 6 is dehydrating tower T103 tower tops
Recycle-water, 7 are mixed amine I, mix the mixture of amine II and diethanolamine column overhead light component, and 8 is E101 condensed fluid, and 9 are
Product monoethanolamine, 10 are monoethanolamine tower T104 tower bottoms and triethanolamine tower T106 tower top light component mixed materials,
11 is diethanolamine tower T105 tower top light components, and 12 is diethanolamine, and 13 is diethanolamine T105 tower bottoms, and 14 is three
Ethanolamine tower T106 tower top light components, 15 is triethanolamine, and 16 is triethanolamine certified products.
In Fig. 1, it is passed through liquid ammonia process for caustic soda purification reactor R101 and is reacted including the raw material of liquefied ammonia and oxirane, product Jing
Mixed amine I is obtained after deamination, ammonia returns liquid ammonia process for caustic soda purification reactor R101 and recycles；It is passed through including the raw material of ammonia and oxirane
Ammonia Process reactor R102 is reacted, and the dehydration of product deamination obtains mixed amine II, and ammonia and water return Ammonia Process reactor
R102 is recycled；Through monoethanolamine tower T104, diethanolamine tower T105, three ethanol after mixed amine I and mixed amine II mixing
Amine tower T106 is refined to obtain product monoethanolamine (MEA), diethanolamine (DEA), triethanolamine (TEA), tower top from side line
Light component is back to previous tower circulation respectively and refines, triethanolamine tower T106 tower reactors extraction triethanolamine certified products.
Below by embodiment, the invention will be further elaborated, but these embodiments are not anyway to the present invention's
Scope is construed as limiting.
Specific embodiment
【Embodiment 1】
It is passed through liquid ammonia process for caustic soda purification reactor R101 and is reacted including the raw material of liquefied ammonia and oxirane, product is Jing after deamination
To mixed amine I, ammonia returns liquid ammonia process for caustic soda purification reactor R101 and recycles；Including the raw material of ammonia and oxirane, to be passed through Ammonia Process anti-
Device R102 is answered to be reacted, the dehydration of product deamination obtains mixed amine II, ammonia and water return Ammonia Process reactor R102 circulations
Utilize；Through monoethanolamine tower T104, diethanolamine tower T105, triethanolamine tower T106 after mixed amine I and mixed amine II mixing
It is refined to obtain product monoethanolamine (MEA), diethanolamine (DEA), triethanolamine (TEA), tower top light component difference from side line
It is back to previous tower circulation refined, triethanolamine tower T106 tower reactors extraction triethanolamine certified products.
Liquid ammonia process for caustic soda purification material molar ratio is ammonia：Oxirane=7.8
Ammonia Process material molar ratio is ammonia：Oxirane=8.5
Ammonia Process reactor operation temperature is 50 DEG C, and pressure is 1.6MPaA, is calculated in mass percent, product composition
For ammonia 65.9%, water 6.6%, ethanolamine 13.2%, diethanolamine 8.8%, triethanolamine 5.5%.
Liquid ammonia process for caustic soda purification reactor operation temperature is 90 DEG C, and pressure is 8.4MPaA, is calculated in mass percent, product composition
For ammonia 69.0%, ethanolamine 14.9%, diethanolamine 13.8%, triethanolamine 2.3%.
Operating pressure 1.3MPaA of ammonia still T101,34 DEG C of tower top temperature, reflux ratio 0.1 are calculated in mass percent,
Tower reactor ammonia<2%.
Operating pressure 1.5MPaA of ammonia still T102,39 DEG C of tower top temperature, reflux ratio 2 are calculated in mass percent, tower
Kettle ammonia<2%.
Operating pressure 100kPaA of dehydrating tower, 39 DEG C of tower top temperature, reflux ratio 1 are calculated in mass percent, tower reactor water<0.1%.
Operating pressure 20kPaA of monoethanolamine tower, 40 DEG C of tower top temperature, reflux ratio 50 are calculated in mass percent, side line
Monoethanolamine>99.9%, moisture<0.1%, colourity<5.
Operating pressure 6kPaA of diethanolamine tower, 170 DEG C of tower top temperature, reflux ratio 30 are calculated in mass percent, side line
Diethanolamine>99.0%, moisture<0.1%, colourity<15.
Operating pressure 0.8kPaA of triethanolamine tower, 142 DEG C of tower top temperature, reflux ratio 10 are calculated in mass percent, side
Line triethanolamine>99.0%, moisture<0.2%, colourity<10；Tower reactor triethanolamine>85%, moisture<0.2%, colourity<30.
In the present embodiment, ammonia still T101, ammonia still T102, dehydrating tower, monoethanolamine tower, diethanolamine tower, three second
The bottom temperature of hydramine tower is equal<180℃.
【Embodiment 2】
Embodiment is same as Example 1, except for the difference that the operating parameter of each tower.
Operating pressure 5MPaA of ammonia still T101,89 DEG C of tower top temperature, reflux ratio 1 are calculated in mass percent, tower reactor
Ammonia<2%.
Operating pressure 5MPaA of ammonia still T102,89 DEG C of tower top temperature, reflux ratio 1 are calculated in mass percent, tower reactor
Ammonia<2%.
Operating pressure 150kPaA of dehydrating tower, 40 DEG C of tower top temperature, reflux ratio 8 are calculated in mass percent, tower reactor water<0.1%.
Operating pressure 30kPaA of monoethanolamine tower, 40 DEG C of tower top temperature, reflux ratio 50 are calculated in mass percent, side line
Monoethanolamine>99.9%, moisture<0.1%, colourity<5.
Operating pressure 1kPaA of diethanolamine tower, 68 DEG C of tower top temperature, reflux ratio 30 are calculated in mass percent, side line
Diethanolamine>99.0%, moisture<0.1%, colourity<10.
Operating pressure 0.3kPaA of triethanolamine tower, 125 DEG C of tower top temperature, reflux ratio 50 are calculated in mass percent, side
Line triethanolamine>99.0%, moisture<0.2%, colourity<10；Tower reactor triethanolamine>85%, moisture<0.2%, colourity<30.
In the present embodiment, ammonia still T101, ammonia still T102, dehydrating tower, monoethanolamine tower, diethanolamine tower, three second
The bottom temperature of hydramine tower is equal<180℃.
【Embodiment 3】
Embodiment is same as Example 1, except for the difference that the operating parameter of each tower.
Operating pressure 1.8MPaA of ammonia still T101,46 DEG C of tower top temperature, reflux ratio 10 are calculated in mass percent,
Tower reactor ammonia<2%.
Operating pressure 2MPaA of ammonia still T102,50 DEG C of tower top temperature, reflux ratio 8 are calculated in mass percent, tower reactor
Ammonia<2%.
Operating pressure 170kPaA of dehydrating tower, 43 DEG C of tower top temperature, reflux ratio 0.5 are calculated in mass percent, tower reactor water
<0.1%.
Operating pressure 3kPaA of monoethanolamine tower, 40 DEG C of tower top temperature, reflux ratio 30 are calculated in mass percent, side line
Monoethanolamine>99.9%, moisture<0.1%, colourity<3.
Operating pressure 0.1kPaA of diethanolamine tower, 52 DEG C of tower top temperature, reflux ratio 40 are calculated in mass percent, side line
Diethanolamine>99.0%, moisture<0.1%, colourity<5.
Operating pressure 0.1kPaA of triethanolamine tower, 128 DEG C of tower top temperature, reflux ratio 80 are calculated in mass percent, side
Line triethanolamine>99.0%, moisture<0.2%, colourity<10；Tower reactor triethanolamine>85%, moisture<0.2%, colourity<30.
In the present embodiment, ammonia still T101, ammonia still T102, dehydrating tower, monoethanolamine tower, diethanolamine tower, three second
The bottom temperature of hydramine tower is equal<180℃.
【Embodiment 4】
Embodiment is same as Example 1, and except for the difference that raw material is different from the operating parameter of each tower.
Liquid ammonia process for caustic soda purification material molar ratio is ammonia：Oxirane=26
Ammonia Process material molar ratio is ammonia：Oxirane=21
Ammonia Process reactor operation temperature is 50 DEG C, and pressure is 1.6MPaA, is calculated in mass percent, product composition
For ammonia 83%, water 3%, ethanolamine 7%, diethanolamine 4%, triethanolamine 3%.
Liquid ammonia process for caustic soda purification reactor operation temperature is 90 DEG C, and pressure is 8.4MPaA, is calculated in mass percent, product composition
For ammonia 88%, ethanolamine 11%, diethanolamine 0.23%, triethanolamine 0.06%.
Operating pressure 3MPaA of ammonia still T101,66 DEG C of tower top temperature, reflux ratio 3 are calculated in mass percent, tower reactor
Ammonia<2%.
Operating pressure 1.3MPaA of ammonia still T102,34 DEG C of tower top temperature, reflux ratio 2 are calculated in mass percent, tower
Kettle ammonia<2%.
Operating pressure 80kPaA of dehydrating tower, 36 DEG C of tower top temperature, reflux ratio 1 are calculated in mass percent, tower reactor water<0.1%.
Operating pressure 12kPaA of monoethanolamine tower, 40 DEG C of tower top temperature, reflux ratio 50 are calculated in mass percent, side line
Monoethanolamine>99.9%, moisture<0.1%, colourity<5.
Operating pressure 5kPaA of diethanolamine tower, 108 DEG C of tower top temperature, reflux ratio 80 are calculated in mass percent, side line
Diethanolamine>99.0%, moisture<0.1%, colourity<15.
Operating pressure 0.5kPaA of triethanolamine tower, 134 DEG C of tower top temperature, reflux ratio 90 are calculated in mass percent, side
Line triethanolamine>99.0%, moisture<0.2%, colourity<10；Tower reactor triethanolamine>85%, moisture<0.2%, colourity<30.
In the present embodiment, ammonia still T101, ammonia still T102, dehydrating tower, monoethanolamine tower, diethanolamine tower, three second
The bottom temperature of hydramine tower is equal<180℃.
【Comparative example 1】
Embodiment is identical with embodiment 1～4, except for the difference that：The operating pressure of monoethanolamine tower is improved to 50kPaA, tower
Kettle temperature degree>180 DEG C, ethanolamine product yield reduces >=1%, and diethanolamine, triethanolamine product colourity increase by 5～40.
Claims (10)
1. a kind of method of liquid ammonia process for caustic soda purification and Ammonia Process co-producing ethanol amine, mainly includes the following steps that：
(1) raw material including liquefied ammonia and oxirane is passed through liquid ammonia process for caustic soda purification reactor and is reacted, and product is obtained Jing after deamination
To mixed amine I, ammonia return liquid ammonia process for caustic soda purification reactor cycles utilization；
(2) raw material including ammonia and oxirane is passed through Ammonia Process reactor and is reacted, product deamination, dehydration
Mixed amine II is obtained, ammonia returns Ammonia Process reactor cycles and utilizes, and water circulation is used as catalyst；
(3) refine from side line through monoethanolamine tower, diethanolamine tower, triethanolamine tower after mixing amine I and mixed amine II mixing
Product monoethanolamine (MEA), diethanolamine (DEA), triethanolamine (TEA) are obtained, tower top light component is back to previous respectively
Individual tower circulation is refined, and triethanolamine tower bottoms is used as triethanolamine certified products.
2. the method for liquid ammonia process for caustic soda purification and Ammonia Process co-producing ethanol amine according to claim 1, it is characterised in that the step (2)
Middle product deamination operation includes ammonia still and recovery ammonia tower.
3. the method for liquid ammonia process for caustic soda purification and Ammonia Process co-producing ethanol amine according to claim 2, it is characterised in that the ammonia still
Operating pressure is 1～5MPaA, and tower top temperature is 30～90 DEG C, and reflux ratio is 0.1～10.
4. the method for liquid ammonia process for caustic soda purification and Ammonia Process co-producing ethanol amine according to claim 2, it is characterised in that the recovery ammonia tower
Operating pressure be 1～5MPaA, tower top temperature be 30～90 DEG C, reflux ratio be 0.1～10.
5. the method for liquid ammonia process for caustic soda purification and Ammonia Process co-producing ethanol amine according to claim 1, it is characterised in that the dehydrating tower
Operating pressure is 0～200kPaA, and tower top temperature is 30～60 DEG C, and reflux ratio is 1～10, and bottom temperature is less than 180 DEG C.
6. the method for liquid ammonia process for caustic soda purification and Ammonia Process co-producing ethanol amine according to claim 1, it is characterised in that the monoethanolamine
The operating pressure of tower is 0～30kPaA, and tower top temperature is 35～60 DEG C, and reflux ratio is 10～100, and bottom temperature is less than 180 DEG C.
7. the method for liquid ammonia process for caustic soda purification and Ammonia Process co-producing ethanol amine according to claim 1, it is characterised in that the diethanol
Amine tower operating pressure is 0～20kPaA, and tower top temperature is 50～150 DEG C, and reflux ratio is 10～100, and bottom temperature is less than 180
℃。
8. the method for liquid ammonia process for caustic soda purification and Ammonia Process co-producing ethanol amine according to claim 1, it is characterised in that the triethanolamine
Tower operating pressure is 0～10kPaA, and tower top temperature is 120-150 DEG C, and reflux ratio is 10～100, and bottom temperature is less than 180 DEG C.
9. the method for liquid ammonia process for caustic soda purification and Ammonia Process co-producing ethanol amine according to claim 1, it is characterised in that the monoethanolamine
Tower, diethanolamine tower, triethanolamine column overhead light component are recycled to previous tower circulation respectively and refine, and overhead condenser is built-in
In or be placed on rectifying column.
10. the method for liquid ammonia process for caustic soda purification and Ammonia Process co-producing ethanol amine according to claim 1, it is characterised in that the ammonia still,
Recovery ammonia tower, dehydrating tower, monoethanolamine tower, diethanolamine tower, the tower reactor reboiler of triethanolamine tower using falling film evaporator,
One kind in climbing film evaporator and luwa evaporator.
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