AU2018101922A4 - Phenyl alkyl sulfonate production plant - Google Patents
Phenyl alkyl sulfonate production plant Download PDFInfo
- Publication number
- AU2018101922A4 AU2018101922A4 AU2018101922A AU2018101922A AU2018101922A4 AU 2018101922 A4 AU2018101922 A4 AU 2018101922A4 AU 2018101922 A AU2018101922 A AU 2018101922A AU 2018101922 A AU2018101922 A AU 2018101922A AU 2018101922 A4 AU2018101922 A4 AU 2018101922A4
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- AU
- Australia
- Prior art keywords
- tank
- kettle
- transfer pump
- alkyl sulfonate
- production plant
- Prior art date
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C303/00—Preparation of esters or amides of sulfuric acids; Preparation of sulfonic acids or of their esters, halides, anhydrides or amides
- C07C303/26—Preparation of esters or amides of sulfuric acids; Preparation of sulfonic acids or of their esters, halides, anhydrides or amides of esters of sulfonic acids
- C07C303/28—Preparation of esters or amides of sulfuric acids; Preparation of sulfonic acids or of their esters, halides, anhydrides or amides of esters of sulfonic acids by reaction of hydroxy compounds with sulfonic acids or derivatives thereof
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C303/00—Preparation of esters or amides of sulfuric acids; Preparation of sulfonic acids or of their esters, halides, anhydrides or amides
- C07C303/02—Preparation of esters or amides of sulfuric acids; Preparation of sulfonic acids or of their esters, halides, anhydrides or amides of sulfonic acids or halides thereof
- C07C303/04—Preparation of esters or amides of sulfuric acids; Preparation of sulfonic acids or of their esters, halides, anhydrides or amides of sulfonic acids or halides thereof by substitution of hydrogen atoms by sulfo or halosulfonyl groups
- C07C303/10—Preparation of esters or amides of sulfuric acids; Preparation of sulfonic acids or of their esters, halides, anhydrides or amides of sulfonic acids or halides thereof by substitution of hydrogen atoms by sulfo or halosulfonyl groups by reaction with sulfur dioxide and halogen or by reaction with sulfuryl halides
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
Phenyl alkyl sulfonate production plant Abstract 5 Phenyl alkyl sulfonate production plant, including: ester oxidation tower (E101), degassing tower (E102), absorption tower (E103), transfer pump (J1O-J104), esterification kettle (DI01), tank (F101), extraction kettle (LIO), tank (F102), tank (F103), distillation column (E104), condenser (ClOl, C102), tank (F104), decolorization kettle (L102), dehydration kettle (L103), pressure filter (L104); among 10 them, tank (FlOl) is used to store waste water, tank (F102) is used to store sodium phenolate, tank (F103) is used to store waste alkali liquor, tank (F104) is used to store neutral oil; among them, transfer pump (JIO) is connected respectively to degassing tower (E102) and esterification kettle (D101), transfer pump (J104) is connected respectively to decolorization kettle (L102) and dehydration kettle (L103); among 15 them, impeller diameter of transfer pump (JIO) is 115-120 mm. Figure 1 -4) Figur I
Description
Phenyl alkyl sulfonate production plant
FIELD OF THE INVENTION
The present invention relates to a kind of pharmaceutical synthesis plant, more particularly, relates to phenyl alkyl sulfonaate production plant.
GENERAL BACKGROUND
Phenyl alkyl sulfonate is auxiliary plasticizer of polyvinyl chloride and vinyl chloride copolymer, with low volatility. Its products have excellent weather ability, physical and mechanical properties and electrical insulation properties, which are suitable for artificial leather, film, wire, cable materials and soles and other products. Cold resistance is less than DOP, dosage is generally 10 to 30 copies. This product can also be used as plasticizer for natural rubber and synthetic rubber to improve the low temperature flexibility and resilience of rubber products. It can be used for food packaging. Most of the existing production plant processes are complex. Thus, as a plasticizer, the advantages and disadvantages of production equipment of phenyl alkyl sulfonate have a great economic significant for improving product quality and reducing the by-product contents.
SUMMARY
The purpose of the present invention is to provide phenyl alkyl sulfonate production plant, including: ester oxidation tower (El01), degassing tower (El02), absorption tower (El03), transfer pump (J101-J104), esterification kettle (DI01), tank (Fl01), extraction kettle (LI01), tank (Fl02), tank (Fl03), distillation column (El04), condenser (C101, Cl02), tank (Fl04), decolorization kettle (LI02), dehydration kettle (LI03), pressure filter (LI04); among them, tank (Fl01) is used to store waste water, tank (Fl02) is used to store sodium phenolate, tank (Fl03) is used to store waste alkali liquor, tank (Fl04) is used to store neutral oil; among them, transfer pump (J101) is connected respectively to degassing tower (El02) and esterification kettle (DI01), transfer pump (JI04) is connected respectively to decolorization kettle (L102) and dehydration kettle (L103); among them, impeller
2018101922 03 Dec 2018 diameter of transfer pump (J101) is 115-120 mm, nominal volume of esterification kettle (D101) is 600-630 L, cone bottom thickness of tank (F102) is 7-8 mm.
Phenyl alkyl sulfonate production plant, the production process is: added the main components of the C12-C18 neutral oil into ester oxidation tower E101, in light, introduced mixture of chlorine gas and sulfur dioxide, absorbed the released hydrogen chloride gas which is generated by the reaction in absorption tower El03 to form hydrochloric acid. Put the materials in degassing tower El02, further driven off the hydrogen chloride gas, absorbed in absorption tower El03 to form hydrochloric acid, then esterification reacted with phenol esterification in esterification kettle D101 under alkaline condition, controlled the feeding temperature at 45-50 °C, time within 30-50 min, after feeding, gradually increased to 70-75 °C, reacted for 1-2 h, run the lower wastewater off, washed the upper crude ester with sodium hydroxide in extraction kettle L101. The washed sodium can be used for the next reaction. Placed the waster alkali liquor in tank Fl03, distilled the washed crude ester with superheated steam in distillation column El04 to remove unreacted liquid wax. Bleached the product by decolorization kettle L102, dehydrated by dehydration kettle L103, filtered by pressure filter LI04, packaged and obtained the finished product. The advantages of this invention are that the reaction time is reduced and the reaction rate is improved. DESCRIPTION OF THE DRAWINGS
Figure 1 is phenyl alkyl sulfonate production plant.
Include: ester oxidation tower (El01), degassing tower (El02), absorption tower (El03), transfer pump (J101-J104), esterification kettle (DI01), tank (Fl01), extraction kettle (LI01), tank (Fl02), tank (Fl03), distillation column (El04), condenser (C101, C102), tank (F104), decolorization kettle (L102), dehydration kettle 25 (LI03), pressure filter (LI04);
DETAILED DESCRIPTION OF PREFERRED EMBODIMENTS
The following examples with reference to specific embodiments of the present invention are further illustrated:
Embodiment 1
Raw materials and dosages
2018101922 03 Dec 2018
| Neutral oil | Take 230-320 °C distillate | 1400 kg | Phenol | First industrial grade, >98% | 600 kg |
| Liquid chlorine | First industrial grade, >99% | 600 kg | Caustic soda | Industrial grade | 1200 kg |
| Sulfur dioxide | First industrial grade, >99% | 600 kg |
Phenyl alkyl sulfonate production plant, including: ester oxidation tower (El01), degassing tower (El02), absorption tower (El03), transfer pump (J101-J104), esterification kettle (DI01), tank (Fl01), extraction kettle (L101), tank (Fl02), tank (Fl 03), distillation column (El 04), condenser (C101, Cl 02), tank (Fl 04), decolorization kettle (L102), dehydration kettle (L103), pressure filter (L104); among them, tank (Fl01) is used to store waste water, tank (Fl02) is used to store sodium phenolate, tank (F103) is used to store waste alkali liquor, tank (F104) is used to store neutral oil; among them, transfer pump (JI01) is connected respectively to degassing tower (El02) and esterification kettle (DI01), transfer pump (JI04) is connected 10 respectively to decolorization kettle (L102) and dehydration kettle (L103); among them, impeller diameter of transfer pump (J101) is 115 mm, nominal volume of esterification kettle (DI 01) is 600 L, cone bottom thickness of tank (Fl 02) is 7 mm.
Phenyl alkyl sulfonate production plant, the production process is: added the main components of the C12-C18 neutral oil into ester oxidation tower E101, in light, 15 introduced mixture of chlorine gas and sulfur dioxide, absorbed the released hydrogen chloride gas which is generated by the reaction in absorption tower El03 to form hydrochloric acid. Put the materials in degassing tower El02, further driven off the hydrogen chloride gas, absorbed in absorption tower El03 to form hydrochloric acid, then esterification reacted with phenol esterification in esterification kettle D101 20 under alkaline condition, controlled the feeding temperature at 45 °C, time within 30 min, after feeding, gradually increased to 70 °C, reacted for 1 h, run the lower wastewater off, washed the upper crude ester with sodium hydroxide in extraction kettle L101. The washed sodium can be used for the next reaction. Placed the waster
2018101922 03 Dec 2018 alkali liquor in tank Fl03, distilled the washed crude ester with superheated steam in distillation column El04 to remove unreacted liquid wax. Bleached the product by decolorization kettle LI02, dehydrated by dehydration kettle LI03, filtered by pressure filter LI04, packaged and obtained the finished product.
The qualities of the product are as follows:
| Exterior | Light yellow oily liquid | Color | <800 |
| Density (25 °C) | 1.04 g/mL | Acidity | <0.02 |
| Refractive index | 1.495 | Viscosity (20 °C) mPa· s | 270 |
| Water solubility | Insoluble in water |
Embodiment 2
Raw materials and dosages
| Neutral oil | Take 230-320 °C distillate | 1500 kg | Phenol | First industrial grade, >98% | 800 kg |
| Liquid chlorine | First industrial grade, >99% | 700 kg | Caustic soda | Industrial grade | 1400 kg |
| Sulfur dioxide | First industrial grade, >99% | 700 kg |
Phenyl alkyl sulfonate production plant, including: ester oxidation tower (El01), degassing tower (El02), absorption tower (El03), transfer pump (JI 01—JI 04), esterification kettle (DI01), tank (Fl01), extraction kettle (LI01), tank (Fl02), tank (Fl 03), distillation column (El 04), condenser (C101, Cl 02), tank (Fl 04), decolorization kettle (L102), dehydration kettle (L103), pressure filter (L104); among them, tank (Fl01) is used to store waste water, tank (Fl02) is used to store sodium phenolate, tank (F103) is used to store waste alkali liquor, tank (F104) is used to store 15 neutral oil; among them, transfer pump (JI01) is connected respectively to degassing tower (El02) and esterification kettle (DI01), transfer pump (JI04) is connected respectively to decolorization kettle (L102) and dehydration kettle (L103); among them, impeller diameter of transfer pump (J101) is 120 mm, nominal volume of esterification kettle (D101) is 630 L, cone bottom thickness of tank (Fl 02) is 8 mm.
2018101922 03 Dec 2018
Phenyl alkyl sulfonate production plant, the production process is: added the main components of the C12-C18 neutral oil into ester oxidation tower E101, in light, introduced mixture of chlorine gas and sulfur dioxide, absorbed the released hydrogen chloride gas which is generated by the reaction in absorption tower El03 to form 5 hydrochloric acid. Put the materials in degassing tower El02, further driven off the hydrogen chloride gas, absorbed in absorption tower El03 to form hydrochloric acid, then esterification reacted with phenol esterification in esterification kettle D101 under alkaline condition, controlled the feeding temperature at 50 °C, time within 50 min, after feeding, gradually increased to 75 °C, reacted for 2 h, run the lower 10 wastewater off, washed the upper crude ester with sodium hydroxide in extraction kettle L101. The washed sodium can be used for the next reaction. Placed the waster alkali liquor in tank Fl03, distilled the washed crude ester with superheated steam in distillation column El04 to remove unreacted liquid wax. Bleached the product by decolorization kettle LI02, dehydrated by dehydration kettle LI03, filtered by 15 pressure filter LI04, packaged and obtained the finished product.
The qualities of the product are as follows:
| Exterior | Light yellow oily liquid | Color | <900 |
| Density (25 °C) | 1.05 g/mL | Acidity | <0.03 |
| Refractive index | 1.497 | Viscosity (20 °C) mPa-s | 290 |
| Water solubility | Insoluble in water |
The embodiments of the present invention are merely preferred embodiments of the present invention, but the range of the present invention is not limited this, and any person who is familiar with those skilled in the arts, within the technical range of the present invention. It is intended that the technical solution and its inventive concept be replaced or modified equivalently with reference to the range of the invention.
Claims (2)
1. Phenyl alkyl sulfonate production plant, including: ester oxidation tower (El01), degassing tower (El02), absorption tower (El03), transfer pump (J101-J104),
5 esterification kettle (DI01), tank (Fl01), extraction kettle (LI01), tank (Fl02), tank (Fl 03), distillation column (El 04), condenser (C101, Cl 02), tank (Fl 04), decolorization kettle (LI02), dehydration kettle (LI03), pressure filter (LI04); among them, tank (Fl01) is used to store waste water, tank (Fl02) is used to store sodium phenolate, tank (F103) is used to store waste alkali liquor, tank (F104) is used to store 10 neutral oil; among them, transfer pump (JI01) is connected respectively to degassing tower (El02) and esterification kettle (DI01), transfer pump (JI04) is connected respectively to decolorization kettle (L102) and dehydration kettle (L103); among them, impeller diameter of transfer pump (JI 01) is 115-120 mm.
2. Phenyl alkyl sulfonate production plant, according to claim 1 wherein nominal
15 volume of esterification kettle (D101) is 600-630 L.3. Phenyl alkyl sulfonate production plant, according to claim 1 wherein cone bottom thickness of tank (Fl 02) is 7-8mm.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201711357621.5A CN108238988A (en) | 2017-12-16 | 2017-12-16 | The process units of phenyl alkylsulf |
| CN2017113576215 | 2017-12-16 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| AU2018101922A4 true AU2018101922A4 (en) | 2019-01-24 |
Family
ID=61158087
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| AU2018101922A Ceased AU2018101922A4 (en) | 2017-12-16 | 2018-12-03 | Phenyl alkyl sulfonate production plant |
Country Status (3)
| Country | Link |
|---|---|
| CN (1) | CN108238988A (en) |
| AU (1) | AU2018101922A4 (en) |
| GB (1) | GB201722049D0 (en) |
-
2017
- 2017-12-16 CN CN201711357621.5A patent/CN108238988A/en not_active Withdrawn
- 2017-12-28 GB GBGB1722049.2A patent/GB201722049D0/en not_active Ceased
-
2018
- 2018-12-03 AU AU2018101922A patent/AU2018101922A4/en not_active Ceased
Also Published As
| Publication number | Publication date |
|---|---|
| GB201722049D0 (en) | 2018-02-14 |
| CN108238988A (en) | 2018-07-03 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| FGI | Letters patent sealed or granted (innovation patent) | ||
| MK22 | Patent ceased section 143a(d), or expired - non payment of renewal fee or expiry |