CN110327967A - The peaceful production. art of the isopropanol of catalyst and preparation method and application catalyst - Google Patents
The peaceful production. art of the isopropanol of catalyst and preparation method and application catalyst Download PDFInfo
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- CN110327967A CN110327967A CN201910681986.6A CN201910681986A CN110327967A CN 110327967 A CN110327967 A CN 110327967A CN 201910681986 A CN201910681986 A CN 201910681986A CN 110327967 A CN110327967 A CN 110327967A
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- catalyst
- isopropanol
- ammonia
- propylene oxide
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- B01J29/40—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11, as exemplified by patent documents US3702886, GB1334243 and US3709979, respectively
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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
- C07C213/04—Preparation of compounds containing amino and hydroxy, amino and etherified hydroxy or amino and esterified hydroxy groups bound to the same carbon skeleton by reaction of ammonia or amines with olefin oxides or halohydrins
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- Crystallography & Structural Chemistry (AREA)
- Engineering & Computer Science (AREA)
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a kind of peaceful production. arts of the isopropanol of catalyst and preparation method and application the catalyst, it is related to isopropanol peace production technical field, manufactured catalyst is packed into reactor, it replaces to oxygen content through nitrogen lower than 0.1%, lead to condition needed for ammonia is warming up to reaction again, the reaction is carried out in gas phase, using continous way process；Propylene oxide is squeezed into carbureter and is reacted with fixed bed reactors are entered after ammonia gas mixture preheating vaporization, reacting rear material is cooled to 15-20 DEG C of progress gas-liquid separation through condenser, and liquid product obtains isopropanolamine series mix products after rectification under vacuum.
Description
Technical field
The present invention relates to isopropanolamine production technical fields more particularly to a kind of catalyst and preparation method and application should
The peaceful production. art of the isopropanol of catalyst.
Background technique
Isopropanolamine can be used as the raw material and fiber industry refining agent, antistatic agent, dyeing assistant and fibre of surfactant
Tie up lubricant, it may also be used for synthetic detergent, cosmetics, lubricating oil, the synthesis for cutting oil, plasticizer, emulsifier；Diisopropanol
Amine is for removing hydrogen sulfide and carbon dioxide in natural gas and refinery gas, for textile auxiliary agent, tanning extracts, insecticide, cutting oil
Deng and relatively broad one of the emulsifier used；Triisopropanolamine is used as medical material, soup solvent.Artificial fibre
Make the solvent of paraffin oil in dimension industry.Since the salt that triisopropanolamine and long chain fatty acids generate has good retention of color,
Therefore the emulsifier particularly useful as cosmetics.
Currently, in the preparation method of isopropanolamine, using propylene oxide and liquefied ammonia as raw material, using water as catalyst.Due to adopting
With high temperature, the reaction condition of High-pressure supercritical, there are very high risk, while because of the presence of water aggravation equipment corrosion, and
And water has also been catalyzed propylene oxide etherificate and has aggregated into high-boiling components, generates solid waste and pollutes environment, feed stock conversion and monoisopropanolamine
Yield is relatively low, in addition, the defects of separating-purifying process need to be dehydrated again and lead to high energy consumption.
Summary of the invention
The invention proposes a kind of peaceful production. arts of the isopropanol of catalyst and preparation method and application the catalyst.
To achieve the goals above, present invention employs following technical solutions:
A kind of catalyst, the component comprising following parts by weight: HZSM-5:96.0%-97.0%, sulfuric acid: 3.0%-
4.0%.
A kind of preparation method of catalyst includes the following steps: to impregnate in the strip HZSM-5 molecular sieve that diameter is 1-3mm
0.5-2 hours in ammonium sulfate, 2-5h is toasted after draining at 100-150 DEG C, finally uses the mixture after baking
400-600 DEG C of high-temperature roasting 5-8h, is made catalyst.
A kind of production technology of isopropanol peace, includes the following steps:
Step 1: manufactured catalyst is packed into reactor, is replaced to oxygen content through nitrogen lower than 0.1%, then logical ammonia
Condition needed for gas lift pressure is warming up to reaction, which carries out in gas phase, using continous way process；
Step 2: squeezing into carbureter for propylene oxide and enters fixed bed reaction after vaporizing with ammonia gas mixture preheating
Device reaction, reacting rear material are cooled to 15-20 DEG C of progress gas-liquid separation through condenser, and liquid product obtains after rectification under vacuum
Isopropanolamine series mix products.
Further, the reaction condition in the step 1 is specially pressure: 0.05~0.3Mpa, reaction temperature:
80~160 DEG C, propylene oxide liquid hourly space velocity: 0.1~1h-1, ammonia and propylene oxide molar ratio: 5.0~50.
Further, in the step 2, the vapor phase ammonia after gas-liquid separation pressurizes through recycle compressor returns to preheating vaporization
Device recycles, and liquid phase samples the pressurized laggard promoting the circulation of qi analysis of hplc of rectifying deamination, obtains mix products.
Further, the mix products in the step 2 include principal product monoisopropanolamine；By-product diisopropyl
Hydramine and triisopropanolamine.
Further, propylene oxide is quantitatively squeezed into carbureter by metering pump in the step 2
Further, the reactor size that the catalyst is packed into is internal diameter 50mm, long 1700mm.
Usefulness: this method uses low pressure reaction, mild condition, and uses the gas-solid under complete anhydrous condition opposite
It answers, not only avoiding leads to that equipment is corroded and separating-purifying process be dehydrated a large amount of energy consumptions of generation again because adding water to be catalyzed,
It avoids propylene oxide etherificate polymerization caused by existing because of water and generates solid waste pollution environment, a small amount of unreacted propylene oxide can be de-
It is thoroughly reacted in ammonia tower, because reducing energy consumption without separating-purifying reuse.And reaction process raw material conversion per pass is high,
Product selectivity is good, and monoisopropanolamine yield is up to 90% or more.
Specific embodiment
The following is a clear and complete description of the technical scheme in the embodiments of the invention, it is clear that described embodiment
Only a part of the embodiment of the present invention, instead of all the embodiments.
Embodiment 1:
91g ammonium sulfate is dissolved in 700ml deionized water, 11.5% ammonium sulfate is made, by 1800g diameter
The strip HZSM-5 molecular sieve of 2mm takes out after impregnating one hour, dries 4 hours through 120 DEG C, and 500 DEG C of muffle furnace roast 6 hours,
Modified catalyst, H is made2SO4Content 3.0%, heap density are 0.67g/ml.Catalyst number is A-1.
Embodiment 2:
According to method described in embodiment 1, ammonium sulfate 152g, water 700ml, HZSM-5 molecular sieve 1800g are taken, is made and is modified
Catalyst.Catalyst number is A-2.
Embodiment 3:
Ammonium sulfate 30g, water 700ml, HZSM-5 molecular sieve 1800g are taken according to method described in embodiment 1, obtained modification is urged
Agent., catalyst number is A-3.
Embodiment 4:
Using the catalyst A-1 in embodiment 1, a kind of production technology of isopropanol peace includes the following steps:
Step 1: the catalyst of manufactured 2732ml is packed into internal diameter 50mm, in the reactor of long 1700mm, is set through nitrogen
Oxygen content is shifted to lower than 0.1%, then logical ammonia is warming up to the required condition of reaction, pressure: 0.15Mpa, reaction temperature: 80
DEG C, propylene oxide liquid hourly space velocity: 0.3h-1, ammonia and propylene oxide molar ratio: 25, which carries out in gas phase, using continous way mistake
Journey；
Step 2: propylene oxide is quantitatively squeezed into carbureter by metering pump and is vaporized with ammonia gas mixture preheating laggard
Enter fixed bed reactors reaction, reacting rear material is cooled to 15-20 DEG C of progress gas-liquid separation through condenser, the gas after gas-liquid separation
Phase ammonia returns to carbureter through recycle compressor pressurization and recycles, and liquid phase samples the pressurized laggard promoting the circulation of qi phase color of rectifying deamination
Spectrum analysis obtains mix products, including principal product monoisopropanolamine；By-product diisopropanolamine (DIPA) and triisopropanolamine.
Embodiment 5:
Using device and method are described in embodiment 4, difference is: concrete operations condition is pressure: 0.15Mpa, instead
Answer temperature: 90 DEG C, propylene oxide liquid hourly space velocity: 0.3h-1, ammonia and propylene oxide molar ratio: 25, catalyst amount: 2732ML.
Embodiment 6:
Using device and method are described in embodiment 4, difference is: concrete operations condition is pressure: 0.15Mpa, instead
Answer temperature: 100 DEG C, propylene oxide liquid hourly space velocity: 0.3h-1, ammonia and propylene oxide molar ratio: 25, catalyst amount: 2732ML.
Embodiment 7:
Using device and method are described in embodiment 4, difference is: concrete operations condition is pressure: 0.15Mpa, instead
Answer temperature: 110 DEG C, propylene oxide liquid hourly space velocity: 0.3h-1, ammonia and propylene oxide molar ratio: 25, catalyst amount: 2732ML.
Embodiment 8:
Using device and method are described in embodiment 4, difference is: concrete operations condition is pressure: 0.15Mpa, instead
Answer temperature: 120 DEG C, propylene oxide liquid hourly space velocity: 0.3h-1, ammonia and propylene oxide molar ratio: 25, catalyst amount: 2732ML.
Embodiment 9:
Using device and method are described in embodiment 4, difference is: concrete operations condition is pressure: 0.15Mpa, instead
Answer temperature: 130 DEG C, propylene oxide liquid hourly space velocity: 0.3h-1, ammonia and propylene oxide molar ratio: 25, catalyst amount: 2732ML.
Embodiment 10:
Using device and method are described in embodiment 4, difference is: concrete operations condition is pressure: 0.05Mpa, instead
Answer temperature: 130 DEG C, propylene oxide liquid hourly space velocity: 0.3h-1, ammonia and propylene oxide molar ratio: 25, catalyst amount: 2732ML.
Embodiment 11:
Using device and method are described in embodiment 4, difference is: concrete operations condition is pressure: 0.30Mpa, instead
Answer temperature: 130 DEG C, propylene oxide liquid hourly space velocity: 0.3h-1, ammonia and propylene oxide molar ratio: 25, catalyst amount: 2732ML.
Embodiment 12:
Using device and method are described in embodiment 4, difference is: concrete operations condition is pressure: 0.15Mpa, instead
Answer temperature: 130 DEG C, propylene oxide liquid hourly space velocity: 0.3h-1, ammonia and propylene oxide molar ratio: 5, catalyst amount: 2732ML.
Embodiment 13:
Using device and method are described in embodiment 4, difference is: concrete operations condition is pressure: 0.15Mpa, instead
Answer temperature: 130 DEG C, propylene oxide liquid hourly space velocity: 0.3h-1, ammonia and propylene oxide molar ratio: 50, catalyst amount: 2732ML.
Embodiment 14:
Using device and method are described in embodiment 4, difference is: using catalyst A- prepared in embodiment 2
2, and concrete operations condition be pressure: 0.15Mpa, reaction temperature: 130 DEG C, propylene oxide liquid hourly space velocity: 0.3h-1, ammonia and epoxy
Propane molar ratio: 25, catalyst amount: 2732ML.
Embodiment 15:
Using device and method are described in embodiment 4, difference is: using catalyst A- prepared in embodiment 3
3, and concrete operations condition be pressure: 0.15Mpa, reaction temperature: 130 DEG C, propylene oxide liquid hourly space velocity: 0.3h-1, ammonia and epoxy
Propane molar ratio: 25, catalyst amount: 2732ML.
Embodiment 16:
Using device and method are described in embodiment 4, difference is: concrete operations condition is pressure: 0.15Mpa, instead
Answer temperature: 140 DEG C, propylene oxide liquid hourly space velocity: 0.3h-1, ammonia and propylene oxide molar ratio: 25, catalyst amount: 2732ML.
Embodiment 17:
Using device and method are described in embodiment 4, difference is: concrete operations condition is pressure: 0.15Mpa, instead
Answer temperature: 150 DEG C, propylene oxide liquid hourly space velocity: 0.3h-1, ammonia and propylene oxide molar ratio: 25, catalyst amount: 2732ML.
Embodiment 18:
Using device and method are described in embodiment 4, difference is: concrete operations condition is pressure: 0.15Mpa, instead
Answer temperature: 160 DEG C, propylene oxide liquid hourly space velocity: 0.3h-1, ammonia and propylene oxide molar ratio: 25, catalyst amount: 2732ML.
The specific reaction condition and result of embodiment 4-18 is listed in table 1.
The reaction condition and result of 1. embodiment 4-18 of table
Embodiment 19:
240 hours stability field investigations are carried out using device and method are described in embodiment 9.With gas chromatographic analysis group
At specific reaction condition and result are listed in table 2.
2. 240 hours stability field investigations of table
From the data in table 2, it can be seen that for the high conversion rate of reaction in 99%, selectivity is higher than 93%, shows to urge under the process conditions
Agent has good stability.
The foregoing is only a preferred embodiment of the present invention, but scope of protection of the present invention is not limited thereto,
Anyone skilled in the art in the technical scope disclosed by the present invention, according to the technique and scheme of the present invention and its
Inventive concept is subject to equivalent substitution or change, should be covered by the protection scope of the present invention.
Claims (8)
1. a kind of catalyst, it is characterised in that: the component comprising following parts by weight: HZSM-5:96.0%-97.0%, sulfuric acid:
3.0%-4.0%.
2. a kind of preparation method of catalyst described in claim 1, characterized by the following steps: by diameter be 1-
The strip HZSM-5 molecular sieve of 3mm is soaked in ammonium sulfate 0.5-2 hours, toasts 2-5h at 100-150 DEG C after draining,
Catalyst finally is made with 400-600 DEG C of high-temperature roasting 5-8h in the mixture after baking.
3. a kind of production technology that the isopropanol using catalyst described in any one in claim 1-2 is pacified, feature exist
In: the following steps are included:
Step 1: manufactured catalyst is packed into reactor, is replaced to oxygen content through nitrogen lower than 0.1%, then logical ammonia liter
Condition needed for pressure is warming up to reaction, which carries out in gas phase, using continous way process；
Step 2: squeezing into carbureter for propylene oxide and it is anti-to enter fixed bed reactors after vaporizing with ammonia gas mixture preheating
It answers, reacting rear material is cooled to 15-20 DEG C of progress gas-liquid separation through condenser, and liquid product obtains isopropyl after rectification under vacuum
Hydramine series mix products.
4. the production technology that the isopropanol of catalyst according to claim 3 is pacified, it is characterised in that: in the step 1
The reaction condition is specially pressure: 0.05~0.3Mpa, reaction temperature: 80~160 DEG C, propylene oxide liquid hourly space velocity: 0.1~
1h-1, ammonia and propylene oxide molar ratio: 5.0~50.
5. the production technology that the isopropanol of catalyst according to claim 3 is pacified, it is characterised in that: in the step 2,
Vapor phase ammonia after gas-liquid separation returns to carbureter through recycle compressor pressurization and recycles, and it is de- that liquid phase samples pressurized rectifying
The laggard promoting the circulation of qi analysis of hplc of ammonia, obtains mix products.
6. the production technology that the isopropanol of catalyst according to claim 3 is pacified, it is characterised in that: in the step 2
The mix products include principal product monoisopropanolamine；By-product diisopropanolamine (DIPA) and triisopropanolamine.
7. the production technology that the isopropanol of catalyst according to claim 3 is pacified, it is characterised in that: will in the step 2
Propylene oxide quantitatively squeezes into carbureter by metering pump.
8. the production technology that the isopropanol of catalyst according to claim 3 is pacified, it is characterised in that: the catalyst is packed into
Reactor size be internal diameter 50mm, long 1700mm.
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110981738A (en) * | 2019-12-30 | 2020-04-10 | 杭州新本立医药有限公司 | Synthesis method of 2-aminopropanol |
| WO2021099456A1 (en) * | 2019-11-20 | 2021-05-27 | Basf Se | Zeolite catalyzed process for the amination of propylene oxide |
| CN114247470A (en) * | 2021-12-31 | 2022-03-29 | 南京红宝丽醇胺化学有限公司 | Preparation method of catalyst and synthesis method of monoisopropanolamine |
| CN114315612A (en) * | 2021-12-27 | 2022-04-12 | 万华化学集团股份有限公司 | Process for continuously producing isopropanolamine |
Citations (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO1998000415A1 (en) * | 1996-07-01 | 1998-01-08 | The Dow Chemical Company | Process for the direct oxidation of olefins to olefin oxides |
| CN1170633A (en) * | 1997-07-24 | 1998-01-21 | 厦门大学 | Catalyst for nonoxidation catalytic dehydrogenation aromatization of methane |
| CN1483713A (en) * | 2003-07-24 | 2004-03-24 | 上海交通大学 | Method for synthesizing beta-ionone |
| CN1623662A (en) * | 2004-10-18 | 2005-06-08 | 中国科学院山西煤炭化学研究所 | Mixed molecular sieve catalyst and its preparation process |
| CN101347739A (en) * | 2007-07-16 | 2009-01-21 | 湖南大学 | Solid acid catalyst and reaction technique for synthesis of allantoin |
| CN101786957A (en) * | 2010-03-24 | 2010-07-28 | 山东东大一诺威新材料有限公司 | Isopropanolamine producing method |
| CN103418235A (en) * | 2013-08-31 | 2013-12-04 | 雷学军 | Device and method for trapping carbon resources in atmosphere |
| CN103936602A (en) * | 2014-04-02 | 2014-07-23 | 四川鑫统领建材科技有限公司 | Method for joint production of isopropanolamine |
| CN104974021A (en) * | 2015-06-29 | 2015-10-14 | 南京林业大学 | Method using sulfuric acid modified nano-level HSZM-5 catalyst to prepare bis(low-carbon alkyloxy)methane |
| CN106631836A (en) * | 2016-11-17 | 2017-05-10 | 北京德博莱化工产品销售有限公司 | Preparation method of novel isopropanolamine |
| WO2018060185A1 (en) * | 2016-09-27 | 2018-04-05 | Basf Se | Method for producing an oxidic composition supported on a carrier material |
| CN109748805A (en) * | 2017-11-01 | 2019-05-14 | 中国石油化工股份有限公司 | The method of liquid ammonia process for caustic soda purification production isopropanolamine |
-
2019
- 2019-07-26 CN CN201910681986.6A patent/CN110327967A/en active Pending
Patent Citations (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO1998000415A1 (en) * | 1996-07-01 | 1998-01-08 | The Dow Chemical Company | Process for the direct oxidation of olefins to olefin oxides |
| CN1170633A (en) * | 1997-07-24 | 1998-01-21 | 厦门大学 | Catalyst for nonoxidation catalytic dehydrogenation aromatization of methane |
| CN1483713A (en) * | 2003-07-24 | 2004-03-24 | 上海交通大学 | Method for synthesizing beta-ionone |
| CN1623662A (en) * | 2004-10-18 | 2005-06-08 | 中国科学院山西煤炭化学研究所 | Mixed molecular sieve catalyst and its preparation process |
| CN101347739A (en) * | 2007-07-16 | 2009-01-21 | 湖南大学 | Solid acid catalyst and reaction technique for synthesis of allantoin |
| CN101786957A (en) * | 2010-03-24 | 2010-07-28 | 山东东大一诺威新材料有限公司 | Isopropanolamine producing method |
| CN103418235A (en) * | 2013-08-31 | 2013-12-04 | 雷学军 | Device and method for trapping carbon resources in atmosphere |
| CN103936602A (en) * | 2014-04-02 | 2014-07-23 | 四川鑫统领建材科技有限公司 | Method for joint production of isopropanolamine |
| CN104974021A (en) * | 2015-06-29 | 2015-10-14 | 南京林业大学 | Method using sulfuric acid modified nano-level HSZM-5 catalyst to prepare bis(low-carbon alkyloxy)methane |
| WO2018060185A1 (en) * | 2016-09-27 | 2018-04-05 | Basf Se | Method for producing an oxidic composition supported on a carrier material |
| CN106631836A (en) * | 2016-11-17 | 2017-05-10 | 北京德博莱化工产品销售有限公司 | Preparation method of novel isopropanolamine |
| CN109748805A (en) * | 2017-11-01 | 2019-05-14 | 中国石油化工股份有限公司 | The method of liquid ammonia process for caustic soda purification production isopropanolamine |
Non-Patent Citations (1)
| Title |
|---|
| 郭玉娟: ""非均相催化合成异丙醇胺工艺研究"", 《中国优秀硕士学位论文全文数据库工程科技Ⅰ辑》 * |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2021099456A1 (en) * | 2019-11-20 | 2021-05-27 | Basf Se | Zeolite catalyzed process for the amination of propylene oxide |
| CN110981738A (en) * | 2019-12-30 | 2020-04-10 | 杭州新本立医药有限公司 | Synthesis method of 2-aminopropanol |
| CN110981738B (en) * | 2019-12-30 | 2022-09-20 | 杭州新本立医药有限公司 | Synthesis method of 2-aminopropanol |
| CN114315612A (en) * | 2021-12-27 | 2022-04-12 | 万华化学集团股份有限公司 | Process for continuously producing isopropanolamine |
| CN114315612B (en) * | 2021-12-27 | 2024-02-02 | 万华化学集团股份有限公司 | Process for continuously producing isopropanolamine |
| CN114247470A (en) * | 2021-12-31 | 2022-03-29 | 南京红宝丽醇胺化学有限公司 | Preparation method of catalyst and synthesis method of monoisopropanolamine |
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Application publication date: 20191015 |