IES20180452A2 - Penetrant n-butyl oleate sodium sulfate production plant - Google Patents
Penetrant n-butyl oleate sodium sulfate production plantInfo
- Publication number
- IES20180452A2 IES20180452A2 IES20180452A2 IE S20180452 A2 IES20180452 A2 IE S20180452A2 IE S20180452 A2 IES20180452 A2 IE S20180452A2
- Authority
- IE
- Ireland
- Prior art keywords
- pump
- tank
- connected respectively
- feedstock
- transfer pump
- Prior art date
Links
- 238000004519 manufacturing process Methods 0.000 title claims description 21
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 title claims description 14
- WIBFFTLQMKKBLZ-SEYXRHQNSA-N n-butyl oleate Chemical compound CCCCCCCC\C=C/CCCCCCCC(=O)OCCCC WIBFFTLQMKKBLZ-SEYXRHQNSA-N 0.000 title claims description 14
- 229910052938 sodium sulfate Inorganic materials 0.000 title claims description 14
- 235000011152 sodium sulphate Nutrition 0.000 title claims description 14
- 238000004821 distillation Methods 0.000 claims description 46
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims description 32
- LRHPLDYGYMQRHN-UHFFFAOYSA-N N-Butanol Chemical compound CCCCO LRHPLDYGYMQRHN-UHFFFAOYSA-N 0.000 claims description 32
- 239000004229 Alkannin Substances 0.000 claims description 20
- 239000002151 riboflavin Substances 0.000 claims description 16
- 239000004149 tartrazine Substances 0.000 claims description 16
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 14
- 238000000605 extraction Methods 0.000 claims description 13
- 238000006386 neutralization reaction Methods 0.000 claims description 12
- ZQPPMHVWECSIRJ-KTKRTIGZSA-N oleic acid Chemical compound CCCCCCCC\C=C/CCCCCCCC(O)=O ZQPPMHVWECSIRJ-KTKRTIGZSA-N 0.000 claims description 9
- 238000006277 sulfonation reaction Methods 0.000 claims description 9
- WRIDQFICGBMAFQ-UHFFFAOYSA-N (E)-8-Octadecenoic acid Natural products CCCCCCCCCC=CCCCCCCC(O)=O WRIDQFICGBMAFQ-UHFFFAOYSA-N 0.000 claims description 7
- LQJBNNIYVWPHFW-UHFFFAOYSA-N 20:1omega9c fatty acid Natural products CCCCCCCCCCC=CCCCCCCCC(O)=O LQJBNNIYVWPHFW-UHFFFAOYSA-N 0.000 claims description 7
- QSBYPNXLFMSGKH-UHFFFAOYSA-N 9-Heptadecensaeure Natural products CCCCCCCC=CCCCCCCCC(O)=O QSBYPNXLFMSGKH-UHFFFAOYSA-N 0.000 claims description 7
- ZQPPMHVWECSIRJ-UHFFFAOYSA-N Oleic acid Natural products CCCCCCCCC=CCCCCCCCC(O)=O ZQPPMHVWECSIRJ-UHFFFAOYSA-N 0.000 claims description 7
- 239000005642 Oleic acid Substances 0.000 claims description 7
- QXJSBBXBKPUZAA-UHFFFAOYSA-N isooleic acid Natural products CCCCCCCC=CCCCCCCCCC(O)=O QXJSBBXBKPUZAA-UHFFFAOYSA-N 0.000 claims description 7
- 239000000047 product Substances 0.000 description 13
- 239000002253 acid Substances 0.000 description 9
- 238000003756 stirring Methods 0.000 description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 6
- 239000003513 alkali Substances 0.000 description 5
- 239000007788 liquid Substances 0.000 description 4
- 239000003054 catalyst Substances 0.000 description 3
- 239000000706 filtrate Substances 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- ZCYVEMRRCGMTRW-UHFFFAOYSA-N 7553-56-2 Chemical compound [I] ZCYVEMRRCGMTRW-UHFFFAOYSA-N 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 2
- 230000008014 freezing Effects 0.000 description 2
- 238000007710 freezing Methods 0.000 description 2
- 229910052740 iodine Inorganic materials 0.000 description 2
- 239000011630 iodine Substances 0.000 description 2
- 150000007524 organic acids Chemical class 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 239000011593 sulfur Substances 0.000 description 2
- 229910052717 sulfur Inorganic materials 0.000 description 2
- 239000004677 Nylon Substances 0.000 description 1
- 229920000297 Rayon Polymers 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000006185 dispersion Substances 0.000 description 1
- 238000004043 dyeing Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000004945 emulsification Methods 0.000 description 1
- 239000000835 fiber Substances 0.000 description 1
- 238000000034 method Methods 0.000 description 1
- 229920001778 nylon Polymers 0.000 description 1
- 230000035515 penetration Effects 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 238000009987 spinning Methods 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 229920002994 synthetic fiber Polymers 0.000 description 1
- 239000012209 synthetic fiber Substances 0.000 description 1
- 239000004753 textile Substances 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 238000009736 wetting Methods 0.000 description 1
- 239000000080 wetting agent Substances 0.000 description 1
Description
FIELD OF THE INVENTION The present invention relates to a kind of pharmaceutical synthesis plant, more particularly, relates to penetrant n-butyl oleate sodium sulfate production plant.
GENERAL BACKGROUND N—butyl oleate sodium sulfate has penetration, emulsification, dispersion, wetting, washing and other properties, has a smooth and cohesive effect for fiber. 1n textile industry, it is used as one of the spinning finishes of synthetic fibers such as nylon and the oil agent of the viscose window line. In the printing and dyeing industry it is used as a wetting agent and softener. Most of the existing production plant processes are complex. Thus, as a penetrant, the advantages and disadvantages of production equipment of n-butyl oleate sodium sulfate 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 penetrant n-butyl oleate sodium sulfate production plant, including: tank (F101), tank (F102), tank (F103), feedstock pump (1101), feedstock pump (J102), feedstock pump (J 103), feedstock pump (J109), knockout drum (L101), reactor (D101), distillation column (E101), transfer pump (J 104), transfer pump (.1105), transfer pump (.1107), transfer pump (J 108), sulfonation kettle (D102), neutralized pump (J 106), neutralization kettle (D103), extraction column (E102), distillation column (E103), product pump (J110), tank (F104); among them, tank (F101) is used to store butanol, tank (F102) is used to store sulfuric acid, tank (F103) is used to store oleic acid, distillation column (E101) is used to store butanol distillation, distillation column (E103) is used to store ethanol distillation, tank (F104) is used to store ethanol; the connection between the various components of the production plant is: feedstock pump (J 101) is connected respectively to tank (F101) and reactor (D101), feedstock pump (J102) is connected respectively to tank (F102) and reactor (D101), feedstock pump (J 103) is connected respectively to tank (F 1 03) and reactor (D101), knockout drum (L101) is connected respectively to reactor (D101) and transfer pump (J 104), distillation column (E101) is connected respectively to transfer pump (J104) and transfer pump (J 105), sulfonation kettle (D102) is connected respectively to transfer pump (J 105) and neutralized pump (J106), neutralization kettle (D103) is connected respectively to neutralized pump (J 106) and transfer pump (J 107),‘ extraction column (E102) is comiected respectively to transfer pump (Jl07), transfer pump (J108), distillation column (E103) and feedstock pump (J 109), feedstock pump (J 109) is connected respectively to tank (F104) and extraction column (E102), distillation colurrm (E103) is connected respectively to transfer pump (J108) and product pump (J110); among them, cylinder diameter of tank (F103) is 450-550 mm, outlet diameter of feedstock pump (J 109) is 170-180 mm, jacket capacity ofreactor (D101) is 230-240 L.
Penetrant n-butyl oleate sodium sulfate production plant, the production process is: added oleic acid and butanol to reactor D101 successively, added sulfuric acid as a catalyst under stirring. Heated, divided by water knockout drum. Raised the temperature above 120-130 "C, distilled excess butanol by E101 distillation column.
Pumped steam to D102 and cooled down to 2-4 "C, added oleum under stirring. After addition, continued to react for 2-3 h, reduced the temperature to 10-15 “C. Then transferred to neutralization kettle D103 which is pre-added water, stirred at 33-36 °C for 2-3 h, rested for 1-2 h, separated the waste acid. Neutralized to the pH value at 5-6 by adding alkali into oil, extracted with ethanol by E102 and filtered off he residue.
Introduced the filtrate into the distillation column E103 steamed out ethanol, got 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 penetrant n-butyl oleate sodium sulfate production plant.
Include: tank (F101), tank (F102), tank (F103), feedstock pump (J101), feedstock pump (J102), feedstock pump (JIO3), feedstock pump (J109), knockout drum (L101), reactor (D101), distillation column (E101), transfer pump (J 104), transfer pump (.1105), transfer pump (J107), transfer pump (J108), sulfonation kettle (D102), neutralized pump (J106), neutralization kettle (D103), extraction column (E102), distillation column (E103), product pump (J1 10), tank (F104); 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 Oleic Industrial grade, freezing 500kg Liquid Industrial 720kg acid point <4 "C alkali grade, 30% Butanol Industrial grade, more than 200kg Ethanol Industrial 500kg 93% distillation at 118 "C grade, 92% Sulfuric Industrial grade, 95% 310kg acid Penetrant n-butyl oleate sodium sulfate production plant, including: tank (F101), tank (F102), tank (F103), feedstock pump (J 101), feedstock pump (J 102), feedstock pump (1103), feedstock pump (J109), knockout drum (L101), reactor (D101), distillation column (E101), transfer pump (J 104), transfer pump (J 105), transfer pump (J107), transfer pump (J108), sulfonation kettle (D102), neutralized pump (J106), neutralization kettle (D103), extraction column (E102), distillation column (E103), product pump (J110), tank (F 104); among them, tank (F101) is used to store butanol, tank (F102) is used to store sulfuric acid, tank (F103) is used to store oleic acid, distillation column (E101) is used to store butanol distillation, distillation column (E103) is used to store ethanol distillation, tank (F104)_is used to store ethanol; the connection between the various components of the production plant is: feedstock pump (J101) is connected respectively to tank (F101) and reactor (D101), feedstock pump (J 102) is connected respectively to tank (F102) and reactor (D101), feedstock pump (J103) is connected respectively to tank (F103) and reactor (D101), knockout drum (L101) is connected respectively to reactor (D101) and transfer pump (J104), distillation column (E101) is connected respectively to transfer pump (J 104) and transfer pump (J 105), sulfonation kettle (D102) is connected respectively to transfer pump (Jl05) and neutralized pump (Jl06), neutralization kettle (D103) is connected respectively to neutralized pump (J 106) and transfer pump (J 107), extraction column (E102) is connected respectively to transfer pump (J107), transfer pump (J108), distillation column (E103) and feedstock pump (J109), feedstock pump (J109) is connected respectively to tank (F104) and extraction column (E102), distillation column (E103) is connected respectively to transfer pump (J 108) and product pump (J 1 10); among them, cylinder diameter of tank (F103) is 450 mm, outlet diameter of feedstock pump (J109) is 170 mm, jacket capacity of reactor (D101) is 230 L.
Penetrant n—butyl oleate sodium sulfate production plant, the production process is: added oleic acid and butanol to reactor D101 successively, added sulfuric acid as a catalyst under stirring. Heated, divided by water knockout drum. Raised the temperature above 120 "C, distilled excess butanol by E101 distillation column.
Pumped steam to D102 and cooled down to 2 °C, added oleum under stirring. After addition, continued to react for 2 h, reduced the temperature to 10 “C. Then transferred to neutralization kettle D103 which is pre-added water, stirred at 33 "C for 2 h, rested for 1 h, separated the waste acid. Neutralized to the pH value at 5 by adding alkali into oil, extracted with ethanol by E102 and filtered off he residue.
Introduced the filtrate into the distillation colurrm E103 steamed out ethanol, got the finished product.
The qualities of the product are as follows: Exterior Red-brown transparent oily liquid pH value 6.7 Organic acid 8%% Acid value 511 mgKOH/g Inorganic sulfur 31.2% Iodine value S 6 glg/kg Moisture 37%% Embodiment 2 Raw materials and dosages Oleic Industrial grade, freezing 500kg Liquid Industrial 750kg acid point <4 °C alkali grade, 30% Butanol Industrial grade, more than 23 0kg Ethanol Industrial 600kg 93% distillation at 118 °C grade, 92% Sulfuric Industrial grade, 95% 350kg acid Penetrant n—butyl oleate sodium sulfate production plant, including: tank (F101), tank (F 102), tank (F103), feedstock pump (J 101), feedstock pump (.1102), feedstock pump (1103), feedstock pump (J 109), knockout drum (L101), reactor (D101), distillation column (E101), transfer pump (JIO4), transfer pump (J105), transfer pump (1107), transfer pump (.1108), sulfonation kettle (D102), neutralized pump (.1106), neutralization kettle (D103), extraction column (E102), distillation column (E103), product pump (J1 10), tank (F104); among them, tank (F101) is used to store butanol, tank (F102) is used to store sulfuric acid, tank (F103) is used to store oleic acid, distillation column (E101) is used to store butanol distillation, distillation column (E103) is used to store ethanol distillation, tank (F104) is used to store ethanol; the connection between the various components of the production plant is: feedstock pump (1101) is connected respectively to tank (F 101) and reactor (D101), feedstock pump (J 102) is connected respectively to tank (F102) and reactor (D101), feedstock pump (1103) is connected respectively to tank (F103) and reactor (D101), knockout drum (L101) is connected respectively to reactor (D101) and transfer pump (J104), distillation column (E101) is connected respectively to transfer pump (.1104) and transfer pump (J 105), sulfonation kettle (D102) is connected respectively toitransfer pump (I105) and neutralized pump (J 106), neutralization kettle (D103) is connected respectively to neutralized pump (J 106) and transfer pump (J 107), extraction column (E102) is connected respectively to transfer pump (J107), transfer pump (J 108), distillation column (E103) and feedstock pump (J109), feedstock pump (J109) is connected respectively to tank (F 104) and extraction column (E102), distillation column (E103) is connected respectively to transfer pump (J108) and product pump (J 1 10); among them, cylinder diameter of tank (F103) is 550 mm, outlet diameter of feedstock pump (J 109) is 180 mm, jacket capacity of reactor (D101) is 240 L.
Penetrant n—butyl oleate sodium sulfate production plant, the production process is: added oleic acid and butanol to reactor D101 successively, added sulfuric acid as a catalyst under stirring. Heated, divided by water knockout drum. Raised the temperature above 130 "C, distilled excess butanol by E101 distillation column.
Pumped steam to D102 and cooled down to 4 "C, added oleum under stirring. After addition, continued to react for 3 h, reduced the temperature to 15 "C. Then transferred to neutralization kettle D103 which is pre-added water, stirred at 36 °C for 3 h, rested for 2 h, separated the waste acid. Neutralized to the pH value at 6 by adding alkali into oil, extracted with ethanol by E102 and filtered olf he residue.
Introduced the filtrate into the distillation column E103 steamed out ethanol, got the finished product.
The qualities of the product are as follows: Exterior Red-brown pH value 6.8 transparent oily liquid Organic acid 9%% Acid value :12 mgKOH/g lnorganic sulfur 31.3% Iodine value S 7 glg/kg Moisture 39%% 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 (3)
1. Penetrant n—butyl oleate sodium sulfate production plant, including: tank (F101), tank (F102), tank (F103), feedstock pump (1101), feedstock pump (1102), feedstock pump (1103), feedstock pump (1109), knockout drum (L101), reactor (D101), distillation column (E101), transfer pump (1104), transfer pump (1105), transfer pump (1107), transfer pump (1108), sulfonation kettle (D102), neutralized pump (1106), neutralization kettle (D103), extraction column (E102), distillation column (E103), product pump (1110), tank (F104); among them, tank (F101) is used to store butanol, tank (F102) is used to store sulfuric acid, tank (F103) is used to store oleic acid, distillation column (E101) is used to store butanol distillation, distillation column (E103) is used to store ethanol distillation, tank (F104) is used to store ethanol; the connection between the various components of the production plant is: feedstock pump (1101) is connected respectively to tank (F 101) and reactor (D101), feedstock pump (1102) is connected respectively to tank (F 102) and reactor (D101), feedstock pump (1103) is connected respectively to tank (F 103) and reactor (D101), knockout drum (L101) is connected respectively to reactor (D101) and transfer pump (1104), distillation column (E101) is connected respectively to transfer pump (1104) and transfer pump (1105), sulfonation kettle (D102) is connected respectively to transfer pump (1105) and neutralized pump (1106), neutralization kettle (D103) is connected respectively to neutralized pump (1106) and transfer pump (1107), extraction column (E102) is connected respectively to transfer pump (1107), transfer pump (1108), distillation column (E103) and feedstock pump (1109), feedstock pump (1109) is connected respectively to tank (F104) and extraction column (E102), distillation column (E103) is connected respectively to transfer pump (1108) and product pump (.11 10); among them, cylinder diameter of tank (F103) is 450-550 mm.
2. Penetrant n—butyl oleate sodium sulfate production plant according to claim 1 wherein outlet diameter of feedstock pump (1109) is 170-180 mm.
3. Penetrant n-butyl oleate sodium sulfate production plant according to claim 1 wherein jacket capacity of reactor (D101) is 230-240 L.
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