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Iso-Butyl Acetate Plant

Iso-Butyl Acetate Plant

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Price:
6000 CNY
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China, Wuhan
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Technical characteristics
  • Country of manufactureChina
Description

Iso-Butyl Acetate Plant

Proprietary Technology and Plants

Technology Introduction:

There are two prevailing processes for iso-butyl acetate (IBA) production, i.e. iso-butanol-acetic acid esterification process and n_butene_acetic acid addition process. Due to its much lower production cost, new IBA plants usually use the Addition Process, which is the very technology SL TECH provides. It consists of four units, feedstock purification unit, esterification unit, product separation unit and acetic acid recovery unit. Compared to the Esterification Process, the Addition Process for IBA production has advantages such as shorter process flow, less equipment and lower production cost (50-60% of Esterification Process); lower energy consumption (only 5% of Esterification Process); easy operation, lower maintenance cost and lower operation cost; harmless and poisonless solid acid catalyst, less pollution, less equipment corrosion.

Technical Features:

  1. Fixed Bed tubular Reactor To ensure the separation effect in the reactor, a disc distributor is arranged at the feedstock inlet; to strengthen the heat exchange effect and better control the temperature in the catalyst bed, baffles are designed in the reactor shell side; to reduce the energy consumption, two pre-heating stages are designed, the first stage is the plate heat exchanger while the second stage is the tubular heat exchanger.
  2. Modified Cation Exchange Resin Catalyst The catalyst is high temperature resistant strong acid resin modified by metal chloride to prolongitself service life. Also after the modification, the conversion yield as weel as the selectivity will be increased at some extent.

Performance:

Product Specification  

S/N

Item

Specification

1

Appearance (Pt-Co)

≦10

2

Density @ 20oC, g/cm3

0.860-0.878

3

Product Purity, wt%

≧97.5

4

Acidity as acetic acid, wt%

≦0.01

5

Water, wt%

≦0.1

6

C-8, wt%

≦2.2

7

others

≦0.1

 

 

 

 

Specific Consumption

Iso-Butyl Acetate Plant

Proprietary Technology and Plants

Technology Introduction:

There are two prevailing processes for iso-butyl acetate (IBA) production, i.e. iso-butanol-acetic acid esterification process and n_butene_acetic acid addition process. Due to its much lower production cost, new IBA plants usually use the Addition Process, which is the very technology SL TECH provides. It consists of four units, feedstock purification unit, esterification unit, product separation unit and acetic acid recovery unit. Compared to the Esterification Process, the Addition Process for IBA production has advantages such as shorter process flow, less equipment and lower production cost (50-60% of Esterification Process); lower energy consumption (only 5% of Esterification Process); easy operation, lower maintenance cost and lower operation cost; harmless and poisonless solid acid catalyst, less pollution, less equipment corrosion.

Technical Features:

  1. Fixed Bed tubular Reactor To ensure the separation effect in the reactor, a disc distributor is arranged at the feedstock inlet; to strengthen the heat exchange effect and better control the temperature in the catalyst bed, baffles are designed in the reactor shell side; to reduce the energy consumption, two pre-heating stages are designed, the first stage is the plate heat exchanger while the second stage is the tubular heat exchanger.
  2. Modified Cation Exchange Resin Catalyst The catalyst is high temperature resistant strong acid resin modified by metal chloride to prolongitself service life. Also after the modification, the conversion yield as weel as the selectivity will be increased at some extent.

Performance:

Product Specification  

S/N

Item

Specification

1

Appearance (Pt-Co)

≦10

2

Density @ 20oC, g/cm3

0.860-0.878

3

Product Purity, wt%

≧97.5

4

Acidity as acetic acid, wt%

≦0.01

5

Water, wt%

≦0.1

6

C-8, wt%

≦2.2

7

others

≦0.1

 

 

 

 

Specific Consumption

S/N

Item

Consumption Rate

1

Acetic Acid (mt/mt @ per ton of 97.5% IBA)

0.55

2

C-4 (mt/mt @ per ton of 97.5% IBA)

0.60

3

Demineralized Water (mt/mt @ per ton of 97.5% IBA)

0.0031

4

Circulating Water (mt/mt @ per ton of 97.5% IBA)

75

5

Fresh Water(mt/mt @ per ton of 97.5% IBA)

0.14

6

Steam(1.5MPaG) (mt/mt @ per ton of 97.5% IBA)

3.70

7

Nitrogen (Nm3/mt @ per ton of 97.5% IBA)

0.71

8

Compressed Air & Instrumental Air 


   (Nm3/mt @ per ton of 97.5% IBA)

 

6.6

9

Electricity (KWH/mt @ per ton of 97.5% IBA)

47

10

Esterification Catalyst (kg/mt @ per ton of 97.5% IBA)

0.55 ( for one load)

S/N

Item

Consumption Rate

1

Acetic Acid (mt/mt @ per ton of 97.5% IBA)

0.55

2

C-4 (mt/mt @ per ton of 97.5% IBA)

0.60

3

Demineralized Water (mt/mt @ per ton of 97.5% IBA)

0.0031

4

Circulating Water (mt/mt @ per ton of 97.5% IBA)

75

5

Fresh Water(mt/mt @ per ton of 97.5% IBA)

0.14

6

Steam(1.5MPaG) (mt/mt @ per ton of 97.5% IBA)

3.70

7

Nitrogen (Nm3/mt

Iso-Butyl Acetate Plant

Proprietary Technology and Plants

Technology Introduction:

There are two prevailing processes for iso-butyl acetate (IBA) production, i.e. iso-butanol-acetic acid esterification process and n_butene_acetic acid addition process. Due to its much lower production cost, new IBA plants usually use the Addition Process, which is the very technology SL TECH provides. It consists of four units, feedstock purification unit, esterification unit, product separation unit and acetic acid recovery unit. Compared to the Esterification Process, the Addition Process for IBA production has advantages such as shorter process flow, less equipment and lower production cost (50-60% of Esterification Process); lower energy consumption (only 5% of Esterification Process); easy operation, lower maintenance cost and lower operation cost; harmless and poisonless solid acid catalyst, less pollution, less equipment corrosion.

Technical Features:

  1. Fixed Bed tubular Reactor To ensure the separation effect in the reactor, a disc distributor is arranged at the feedstock inlet; to strengthen the heat exchange effect and better control the temperature in the catalyst bed, baffles are designed in the reactor shell side; to reduce the energy consumption, two pre-heating stages are designed, the first stage is the plate heat exchanger while the second stage is the tubular heat exchanger.
  2. Modified Cation Exchange Resin Catalyst The catalyst is high temperature resistant strong acid resin modified by metal chloride to prolongitself service life. Also after the modification, the conversion yield as weel as the selectivity will be increased at some extent.

Performance:

Product Specification  

S/N

Item

Specification

1

Appearance (Pt-Co)

≦10

2

Density @ 20oC, g/cm3

0.860-0.878

3

Product Purity, wt%

≧97.5

4

Acidity as acetic acid, wt%

≦0.01

5

Water, wt%

≦0.1

6

C-8, wt%

≦2.2

7

others

≦0.1

 

 

 

 

Specific Consumption

S/N

Item

Consumption Rate

1

Acetic Acid (mt/mt @ per ton of 97.5% IBA)

0.55

2

C-4 (mt/mt @ per ton of 97.5% IBA)

0.60

3

Demineralized Water (mt/mt @ per ton of 97.5% IBA)

0.0031

4

Circulating Water (mt/mt @ per ton of 97.5% IBA)

75

5

Fresh Water(mt/mt @ per ton of 97.5% IBA)

0.14

6

Steam(1.5MPaG) (mt/mt @ per ton of 97.5% IBA)

3.70

7

Nitrogen (Nm3/mt @ per ton of 97.5% IBA)

0.71

8

Compressed Air & Instrumental Air 


   (Nm3/mt @ per ton of 97.5% IBA)

 

6.6

9

Electricity (KWH/mt @ per ton of 97.5% IBA)

47

10

Esterification Catalyst (kg/mt @ per ton of 97.5% IBA)

0.55 ( for one load)

@ per ton of 97.5% IBA)

0.71

8

Compressed Air & Instrumental Air 


   (Nm3/mt @ per ton of 97.5% IBA)

 

6.6

9

Electricity (KWH/mt @ per ton of 97.5% IBA)

47

10

Esterification Catalyst (kg/mt @ per ton of 97.5% IBA)

0.55 ( for one load)

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