CN103396894A - Fatty acid rectification separation method - Google Patents
Fatty acid rectification separation method Download PDFInfo
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- CN103396894A CN103396894A CN2013103722880A CN201310372288A CN103396894A CN 103396894 A CN103396894 A CN 103396894A CN 2013103722880 A CN2013103722880 A CN 2013103722880A CN 201310372288 A CN201310372288 A CN 201310372288A CN 103396894 A CN103396894 A CN 103396894A
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Abstract
The invention relates to a fatty acid rectification separation method. The fatty acid rectification separation method is characterized in that a separation tower used for the fatty acid rectification separation method is filled with ceramic plate corrugated packings. The fatty acid rectification separation method is particularly as follows: fatty acid enters the separation tower from an intermediate part under the condition of vacuum, light component fatty acid is separated from a tower top, and heavy component fatty acid is separated from a tower bottom; the lower section of the separation tower is a stripping section, the upper section of the separation tower is a rectifying section, and the stripping section and the rectifying section are respectively filled with the ceramic plate corrugated packings; a direct-connected condenser is arranged on the tower top; a reboiler and a circulation pump used for forced circulation are arranged at the tower bottom; the carbon number of the fatty acid is 8-22, and the fatty acid is saturated or unsaturated animal and vegetable oil fatty acid. According to the fatty acid rectification separation method disclosed by the invention, the ceramic plate corrugated packings have good corrosion resistance, are low in cost and can be used all the year round without being replaced, so that the initial investment cost and the maintenance cost are reduced; the metal packings are prevented from influencing the quality of products because corroding metal ions enter the products. The fatty acid rectification separation method disclosed by the invention has the advantages of good quality and low cost of produced products, and the economic benefit is increased.
Description
Technical field
The present invention relates to the oil and fat chemical field, particularly a kind of lipid acid distillation and separation method.
Background technology
Natural acid is not generally to exist with single lipid acid, but the mixture of Fatty acid homologue, for meeting the different needs, need be separated.Fatty acid separation has freezing milling process, tensio-active agent emulsion process and solvent separation, but product purity is not high, labour intensity is large, cost is high, small scale.what technical scale was commonly used is continuous rectification under vacuum isolation technique, utilize the difference of its component boiling point and relative volatility to separate, industrial high efficiency low pressure drop Lamb wave line metallic stuffing knockout tower is widely applied, because lipid acid has temperature-sensitive, oxidation and corrodibility, at high temperature has very strong corrodibility, in actual production process, the core knockout tower stainless steel plate ripple packing life-span of this technology is very short and valency is high, only have about 1 year as 00Cr17Ni14Mo6 and C15 high-alloy stainless steel Mellapak packing life-span, only 3-6 month 316L stainless steel plate ripple packing life-span, can't steady in a long-termly produce, upkeep cost and production cost rise, the metal ion that also due to the Corrosion of Stainless Steel process, produces enters into product and causes product variable color and metal ion to exceed standard, affect product quality, limit its purposes.For solving this agricultural technology problem, need a kind of can steady in a long-termly production, do not affect the lipid acid distillation and separation method of separating effect and polluted product.
Summary of the invention
, in order to overcome above-mentioned defect, the invention provides a kind of lipid acid distillation and separation method.The invention is characterized in and load onto the ceramic plate ripple packing in the knockout tower of lipid acid rectifying separation.
The technology of the present invention technique is as follows: lipid acid enters from the knockout tower middle part under vacuum condition, and tower top is isolated light constituent lipid acid, isolates heavy constituent lipid acid at the bottom of tower; At the bottom of tower top light constituent and tower, heavy constituent all adopts the discharging of high bit gravity nature.
Described knockout tower is: hypomere is stripping section, and epimere is rectifying section, and the ceramic plate ripple packing is housed respectively, and tower top is furnished with the associated mode condenser, is furnished with the recycle pump that reboiler and pump circulation are used at the bottom of tower.
At the bottom of described tower top light constituent and tower, heavy constituent all adopts the discharging of high bit gravity nature to be: between discharge port and product receiving tank, difference of altitude is greater than more than 10 meters, and material gravity is enough to overcome vacuum system and atm difference, by liquid seal device natural discharging continuously.
Concrete step is as follows:
Under vacuum condition, absolute pressure 1-800pa, be preferably 5-500pa, the lipid acid acid through dewatering degassed enters from the knockout tower middle part, controls feeding temperature 40-240 ℃, be preferably 100-230 ℃, control bottom temp 200-270 ℃, head temperature 50-230 ℃, overhead product are light constituent, the bottom component is heavy constituent, by high bit gravity nature discharging extraction from vacuum system.
Wherein said lipid acid is the animal and plant fatty acid oil, and carbochain is distributed as the saturated and unsaturated fatty acids of 8-22 carbon.
Positively effect of the present invention:
A kind of lipid acid distillation and separation method of the present invention, ceramic plate ripple packing good corrosion resistance, inexpensive, can use all the year round and need not to change, and guaranteed device operation steady in a long-term, reduce first the input and maintenance cost, avoid keeping in repair the direct and indirect economic loss that stops and cause; Avoid metallic stuffing to affect product quality because the corroding metal ion enters product.The good product quality that the method is produced, cost is low, has widened the product application scope, has improved economic benefit.
In addition, in the present invention, the discharging of high bit gravity nature is all adopted in the material extraction, avoids the air suck-back to enter vacuum system accidents caused, does not need pump to extract, do not increase energy consumption, continuous discharge and safe and reliable out.The knockout tower tower top is furnished with the associated mode condenser, and compact construction, material stroke are short, have advantages of energy-conservation and pressure drop low; Be furnished with the recycle pump vaporization efficiency that reboiler and pump circulation use at the bottom of tower high, can reduce the temperature difference between heating agent and material, reduce heat-sensitive substance thermolysis and polymerization, lower heat medium temperature helps to reduce energy consumption.
Description of drawings
Fig. 1. lipid acid rectifying separation system schematic: 1, knockout tower, 2, the stripping section filler, 3, the rectifying section filler, 4, condenser; 5, circulation tube; 6, recycle pump; 7, reboiler; 8, feed-pipe; 9, light constituent discharge nozzle; 10, heavy constituent discharge nozzle; 11, U-shaped liquid seal device; 12, reboiler pipe connecting; 13, thermometer.
Embodiment
Be below specific embodiments of the invention, further describe the present invention, but the present invention be not limited only to this.
In following examples, separation method is all used separation system as shown in Figure 1.
A kind of lipid acid distillation and separation method of the present invention, concrete steps are as follows:
Be under the 50-500pa vacuum condition in absolute pressure, degassed through dewatering
Oleum Gossypii semenLipid acid acid enters from the knockout tower middle part, control feeding temperature 150-220 ℃, control bottom temp 235-250 ℃, head temperature 150-225 ℃, overhead product is that C16 content is the light constituent of 96-99%, for palmitinic acid (having another name called Palmiticacid), product is white powder, free from extraneous odour, fusing point 61-63 ℃, acid value 210-228mgKOH/g; The bottom component is that C18 content is the heavy constituent of 98-99.5%, is Oleum Gossypii semen oleic acid, and product color (Fe-Co colorimetric) is 2#, acid value 198-205mgKOH/g, iodine value 140-145gI
2/ 100g, Fe ion content are less than 0.0005%, and product is all by high bit gravity nature discharging extraction from vacuum system.
Embodiment 2
A kind of lipid acid distillation and separation method of the present invention, concrete steps are as follows:
Be under the 50-500pa vacuum condition in absolute pressure, degassed through dewatering
Soybean oilLipid acid acid enters from the knockout tower middle part, control feeding temperature 150-220 ℃, control bottom temp 240-255 ℃, head temperature 150-225 ℃, overhead product is that C16 content is the light constituent of 96-99%, for palmitinic acid (having another name called Palmiticacid), product is white powder, free from extraneous odour, fusing point 60-62 ℃, acid value 210-228mgKOH/g; The bottom component is that C18 content is the heavy constituent of 98-99.5%, is soybean oil oleic acid, and product color (Fe-Co colorimetric) is 1#, acid value 196-203mgKOH/g, iodine value 143-148gI
2/ 100g, Fe ion content are less than 0.0005%, and product is all by high bit gravity nature discharging extraction from vacuum system.
Embodiment 3
A kind of lipid acid distillation and separation method of the present invention, concrete steps are as follows:
Be under the 50-500pa vacuum condition in absolute pressure, degassed through dewatering
Rapeseed oilLipid acid acid enters from the knockout tower middle part, control feeding temperature 150-220 ℃, control 245-265 ℃ of head temperature 150-225 ℃ of bottom temp, overhead product is that C16 content is the light constituent of 96-99%, for palmitinic acid (having another name called Palmiticacid), product is white powder, free from extraneous odour, fusing point 60-62 ℃, acid value 210-228mgKOH/g; The bottom component is that C18 content is the heavy constituent of 98-99.5%, is rapeseed oil oleic acid, and product color (Fe-Co colorimetric) is 1#, acid value 195-202mgKOH/g, iodine value 120-133gI
2/ 100g, Fe ion content are less than 0.0005%, and product is all by high bit gravity nature discharging extraction from vacuum system.
Claims (4)
1. a lipid acid distillation and separation method, is characterized in that, in this separation method knockout tower used, the ceramic plate ripple packing is housed.
2. separation method as claimed in claim 1 is characterized in that the method is:
Lipid acid enters from the knockout tower middle part under vacuum condition, and tower top is isolated light constituent lipid acid, isolates heavy constituent lipid acid at the bottom of tower;
Described knockout tower is: hypomere is stripping section, and epimere is rectifying section, and the ceramic plate ripple packing is housed respectively;
Tower top is furnished with the associated mode condenser, joins the recycle pump that reboiler and pump circulation are used at the bottom of tower;
The carbon number of described lipid acid is 8-22.
3. separation method as claimed in claim 1 is characterized in that the concrete step of the method is as follows:
Under vacuum condition, absolute pressure 1-800pa, be preferably 5-500pa, enter from the knockout tower middle part through the degassed lipid acid that dewaters, control feeding temperature 40-240 ℃, be preferably 100-230 ℃, control 200-270 ℃ of head temperature 50-230 ℃ of bottom temp, overhead product is light constituent, and the bottom component is heavy constituent, by high bit gravity nature discharging extraction from vacuum system.
4. separation method as claimed in claim 1, is characterized in that described lipid acid is saturated and undersaturated animal and plant fatty acid oil.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201310372288.0A CN103396894B (en) | 2013-08-24 | 2013-08-24 | Fatty acid rectification separation method |
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| CN201310372288.0A CN103396894B (en) | 2013-08-24 | 2013-08-24 | Fatty acid rectification separation method |
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| CN103396894A true CN103396894A (en) | 2013-11-20 |
| CN103396894B CN103396894B (en) | 2015-02-11 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104311410A (en) * | 2014-10-13 | 2015-01-28 | 南京大学 | Method for continuously refining fatty acid |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101033180A (en) * | 2007-04-12 | 2007-09-12 | 上海华谊丙烯酸有限公司 | Fractionating tower for separating acrylic aldehyde from 3-hydroxypropionaldehyde solution |
| CN202410677U (en) * | 2011-12-09 | 2012-09-05 | 刘裕秋 | Foamed ceramic structured ripple packing |
| CN102703222A (en) * | 2012-05-30 | 2012-10-03 | 常州大学 | Method for separating mixed fatty acid by separating wall distillation tower |
-
2013
- 2013-08-24 CN CN201310372288.0A patent/CN103396894B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101033180A (en) * | 2007-04-12 | 2007-09-12 | 上海华谊丙烯酸有限公司 | Fractionating tower for separating acrylic aldehyde from 3-hydroxypropionaldehyde solution |
| CN202410677U (en) * | 2011-12-09 | 2012-09-05 | 刘裕秋 | Foamed ceramic structured ripple packing |
| CN102703222A (en) * | 2012-05-30 | 2012-10-03 | 常州大学 | Method for separating mixed fatty acid by separating wall distillation tower |
Non-Patent Citations (3)
| Title |
|---|
| 徐季亮: "采用陶瓷波纹填料塔回收乙醇", 《江苏化工.市场七日讯》 * |
| 徐立等: "陶瓷波纹填料在氯仿精馏中的应用", 《中国氯碱》 * |
| 陈春林: "工业规模连续减压精馏分离脂肪酸", 《精细石油化工》 * |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104311410A (en) * | 2014-10-13 | 2015-01-28 | 南京大学 | Method for continuously refining fatty acid |
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