CN101423232A - Separation method of sodium sulfate salt and glycerol in 12-hydroxytearic acid production waste liquid - Google Patents
Separation method of sodium sulfate salt and glycerol in 12-hydroxytearic acid production waste liquid Download PDFInfo
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- CN101423232A CN101423232A CNA2008101599626A CN200810159962A CN101423232A CN 101423232 A CN101423232 A CN 101423232A CN A2008101599626 A CNA2008101599626 A CN A2008101599626A CN 200810159962 A CN200810159962 A CN 200810159962A CN 101423232 A CN101423232 A CN 101423232A
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Abstract
The invention belongs to the methods for producing 12-hydroxystearic acid by using castor oil as raw material, and particularly relates to a separation method of by-product sodium sulfate and glycerine. The separation method of the sodium sulfate and the glycerine uses a production process of connecting dual-effect evaporation and single-effect evaporation in series and carries out the separation of the sodium sulfate after saponification and the acidolysis and glycerinated water, the glycerinated water is firstly evaporated by a dual-effect evaporator and then evaporated by a single-effect evaporator, then crude glycerine and bottom materials with very high solid content are obtained, and the bottom materials are centrifugalized and dried to obtain the sodium sulfate. The separation method has the advantages that the separation method can fully recover and utilize the glycerine, the sodium sulfate and other useful chemical substances which are contained in the glycerinated water, water and heat energy during the separation process can be repeatedly utilized, thereby greatly reducing the discharge amount of sewage.
Description
Technical field
The invention belongs to the Viscotrol C is the method for raw material production 12-oxystearic acid, is specially the separation method of by-product sodium sulfate salt and glycerine.
Background technology
Glycerine Chinese: glycerol, molecular formula: C
3H
8O
3, colourless viscous liquid, odorlessness, pleasantly sweet, can the moisture absorption.Be used for gas-chromatography stationary liquid and organic synthesis, also can be used as solvent, tolerance and take into account water pressure engine shock absorber fluid, tenderizer, antibiotic fermentation with nutrition agent, siccative etc.Glycerine is the framework ingredient of tri-glyceride molecule, and when human body was taken in edible-fat, tri-glyceride wherein decomposed through internal metabolism, and formation glycerine also is stored in the adipocyte.
The sodium sulfate salt Chinese: sodium sulfate is used to make water glass, glass, enamel, paper pulp, refrigeration mixture, washing composition, siccative, dye-dilution agent, analytical chemistry reagent, pharmaceuticals etc.
At present, sodium sulfate salt, the glycerol liquor of by-product all are directly to discharge with the form of waste water in the domestic 12-oxystearic acid production technique, not only cause environmental pollution, and sodium sulfate salt, glycerin extraction do not come out to cause the significant wastage of the resources of production.
Summary of the invention
Purpose of the present invention is exactly that a kind of method of producing separating sodium sulfate salt and glycerine in the waste liquid from the 12-oxystearic acid is provided at the defective of above-mentioned existence, adopt this separation method, advantage is fully to recycle useful chemical substances such as the glycerine that contains in the glycerol liquor, sodium sulfate salt, and, significantly reduce the sewage emissions amount with water in the sepn process and heat recycling.
Technical scheme of the present invention is: the waste liquid after the saponification acidolysis is commonly called as glycerol liquor and is stored in the glycerol liquor basin, with pump preheater is preheated to 70 ℃-80 ℃ glycerol liquor and pumps into the 2nd effect evaporator evaporation, vaporization temperature is 90 ℃-100 ℃, feed liquid in the 2nd effect evaporator is pumped to wet cyclone with adopting salt, crystal salt enters salt, glycerine header tank after thickening, clear liquid enters 1st effective evaporator; The temperature of 1st effective evaporator is 100 ℃-110 ℃, and the feed liquid of 1st effective evaporator is delivered to wet cyclone through discharging pump, enters salt, glycerine header tank after the crystal salt thickening, in the clear liquid glycerol content reach 50% with top discharge to the raw glycerine jar; Feed liquid in salt, the glycerine header tank is through whizzer charge pump, wet cyclone, solid content enters whizzer at the bed material more than 60%, clear liquid is got back to header tank, mother liquor after whizzer separates flows into the mother liquor pond, squeeze into the glycerol liquor basin with the mother liquor pump then, isolated crystal salt can pack after the drying by the transmission dehumidification system of taking.
Living steam from boiler enters the 2nd effect evaporator heating chamber, water of condensation goes to flow into hot tub after glycerol liquor preheater and the glycerol liquor heat exchange through drain trap, the secondary steam that 2nd effect evaporator steams is caught through the two-stage eddy flow and is removed the 1st effective evaporator heating chamber after fog separates, water of condensation is through the trap water pot that reduces phlegm and internal heat, the secondary steam of 1st effective evaporator is absorbed by the atmosphere condensation after two-stage eddy flow spray catcher separates.
Beneficial effect of the present invention is: used the placed in-line production technique of two-effect evaporation and single-effect evaporation, with the sodium sulfate salt after the saponification acidolysis, glycerol liquor separates, " waste water " is decomposed into sodium sulfate salt, smart two kinds of final products of glycerine and distilled water, distilled water is as the process water of other operations, glycerine and sodium sulfate salt have been obtained, 1 ton of 12-oxystearic acid of every production just can obtain 60 kilograms of glycerine, 200 kilograms of sodium sulfate salts, at first reached the zero release of waste water, greatly reduce pollution, secondly reclaim the chemical products that obtains, increase the extra earning of enterprise environment, and indirect saving production cost, after in a word glycerol liquor being carried out separating treatment, energy-saving and emission-reduction, the country that meets the energy-saving and emission-reduction of advocating at present calls.
Embodiment
Below in conjunction with specific embodiment technical scheme of the present invention is described in detail.
Embodiment 1
Glycerol liquor after the saponification acidolysis is stored in the glycerol liquor basin, with pump preheater is preheated to 80 ℃ glycerol liquor and pumps into the 2nd effect evaporator evaporation, vaporization temperature is 100 ℃, feed liquid in the 2nd effect evaporator is pumped to wet cyclone with adopting salt, crystal salt enters salt, glycerine header tank after thickening, clear liquid enters 1st effective evaporator; The temperature of 1st effective evaporator is 110 ℃, and the feed liquid of 1st effective evaporator is delivered to wet cyclone through discharging pump, enters salt, glycerine header tank after the crystal salt thickening, in the clear liquid glycerol content reach 50% with top discharge to the raw glycerine jar; Feed liquid in salt, the glycerine header tank is through whizzer charge pump, wet cyclone, solid content enters whizzer at the bed material more than 60%, clear liquid is got back to header tank, mother liquor after whizzer separates flows into the mother liquor pond, squeeze into the glycerol liquor basin with the mother liquor pump then, isolated crystal salt can pack after the drying by the transmission dehumidification system of taking.
Embodiment 2
Glycerol liquor after the saponification acidolysis is stored in the glycerol liquor basin, with pump preheater is preheated to 70 ℃ glycerol liquor and pumps into the 2nd effect evaporator evaporation, vaporization temperature is 90 ℃, feed liquid in the 2nd effect evaporator is pumped to wet cyclone with adopting salt, crystal salt enters salt, glycerine header tank after thickening, clear liquid enters 1st effective evaporator; The temperature of 1st effective evaporator is 100 ℃, and the feed liquid of 1st effective evaporator is delivered to wet cyclone through discharging pump, enters salt, glycerine header tank after the crystal salt thickening, in the clear liquid glycerol content reach 50% with top discharge to the raw glycerine jar; Feed liquid in salt, the glycerine header tank is through whizzer charge pump, wet cyclone, solid content enters whizzer at the bed material more than 60%, clear liquid is got back to header tank, mother liquor after whizzer separates flows into the mother liquor pond, squeeze into the glycerol liquor basin with the mother liquor pump then, isolated crystal salt can pack after the drying by the transmission dehumidification system of taking.
Claims (3)
1.12-the separation method of sodium sulfate salt and glycerine in the oxystearic acid production waste liquid, it is characterized in that, glycerol liquor after the saponification acidolysis is stored in the glycerol liquor basin, with pump preheater is preheated to 70 ℃-80 ℃ glycerol liquor and pumps into the 2nd effect evaporator evaporation, vaporization temperature is 90 ℃-100 ℃, feed liquid in the 2nd effect evaporator is pumped to wet cyclone with adopting salt, and crystal salt enters salt, glycerine header tank after thickening, and clear liquid enters 1st effective evaporator; The temperature of 1st effective evaporator is 100 ℃-110 ℃, and the feed liquid of 1st effective evaporator is delivered to wet cyclone through discharging pump, enters salt, glycerine header tank after the crystal salt thickening, in the clear liquid glycerol content reach 50% with top discharge to the raw glycerine jar; Feed liquid in salt, the glycerine header tank is through whizzer charge pump, wet cyclone, solid content enters whizzer at the bed material more than 60%, clear liquid is got back to header tank, mother liquor after whizzer separates flows into the mother liquor pond, squeeze into the glycerol liquor basin with the mother liquor pump then, isolated crystal salt can pack after the drying by the transmission dehumidification system of taking.
2. the separation method of sodium sulfate salt and glycerine in the 12-oxystearic acid production waste liquid according to claim 1, it is characterized in that, glycerol liquor after the saponification acidolysis is stored in the glycerol liquor basin, with pump preheater is preheated to 80 ℃ glycerol liquor and pumps into the 2nd effect evaporator evaporation, vaporization temperature is 100 ℃, feed liquid in the 2nd effect evaporator is pumped to wet cyclone with adopting salt, and crystal salt enters salt, glycerine header tank after thickening, and clear liquid enters 1st effective evaporator; The temperature of 1st effective evaporator is 110 ℃, and the feed liquid of 1st effective evaporator is delivered to wet cyclone through discharging pump, enters salt, glycerine header tank after the crystal salt thickening, in the clear liquid glycerol content reach 50% with top discharge to the raw glycerine jar; Feed liquid in salt, the glycerine header tank is through whizzer charge pump, wet cyclone, solid content enters whizzer at the bed material more than 60%, clear liquid is got back to header tank, mother liquor after whizzer separates flows into the mother liquor pond, squeeze into the glycerol liquor basin with the mother liquor pump then, isolated crystal salt can pack after the drying by the transmission dehumidification system of taking.
3. the separation method of sodium sulfate salt and glycerine in the 12-oxystearic acid production waste liquid according to claim 1, it is characterized in that, glycerol liquor after the saponification acidolysis is stored in the glycerol liquor basin, with pump preheater is preheated to 70 ℃ glycerol liquor and pumps into the 2nd effect evaporator evaporation, vaporization temperature is 90 ℃, feed liquid in the 2nd effect evaporator is pumped to wet cyclone with adopting salt, and crystal salt enters salt, glycerine header tank after thickening, and clear liquid enters 1st effective evaporator; The temperature of 1st effective evaporator is 100 ℃, and the feed liquid of 1st effective evaporator is delivered to wet cyclone through discharging pump, enters salt, glycerine header tank after the crystal salt thickening, in the clear liquid glycerol content reach 50% with top discharge to the raw glycerine jar; Feed liquid in salt, the glycerine header tank is through whizzer charge pump, wet cyclone, solid content enters whizzer at the bed material more than 60%, clear liquid is got back to header tank, mother liquor after whizzer separates flows into the mother liquor pond, squeeze into the glycerol liquor basin with the mother liquor pump then, isolated crystal salt can pack after the drying by the transmission dehumidification system of taking.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA2008101599626A CN101423232A (en) | 2008-11-14 | 2008-11-14 | Separation method of sodium sulfate salt and glycerol in 12-hydroxytearic acid production waste liquid |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA2008101599626A CN101423232A (en) | 2008-11-14 | 2008-11-14 | Separation method of sodium sulfate salt and glycerol in 12-hydroxytearic acid production waste liquid |
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| Publication Number | Publication Date |
|---|---|
| CN101423232A true CN101423232A (en) | 2009-05-06 |
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|---|---|---|---|
| CNA2008101599626A Pending CN101423232A (en) | 2008-11-14 | 2008-11-14 | Separation method of sodium sulfate salt and glycerol in 12-hydroxytearic acid production waste liquid |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102260141A (en) * | 2010-05-25 | 2011-11-30 | 中国林业科学研究院林产化学工业研究所 | Production method and device of refined glycerin in non-distillation techniques |
| CN102757153A (en) * | 2012-07-12 | 2012-10-31 | 山东天兴生物科技有限公司 | Method for treating wastewater generated during production of 12-hydroxy stearic acid |
| CN104445721A (en) * | 2014-11-19 | 2015-03-25 | 南通新邦化工科技有限公司 | Combined treatment method for stearate wastewater |
-
2008
- 2008-11-14 CN CNA2008101599626A patent/CN101423232A/en active Pending
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102260141A (en) * | 2010-05-25 | 2011-11-30 | 中国林业科学研究院林产化学工业研究所 | Production method and device of refined glycerin in non-distillation techniques |
| CN102260141B (en) * | 2010-05-25 | 2013-11-27 | 中国林业科学研究院林产化学工业研究所 | Production method and device of refined glycerin in non-distillation techniques |
| CN102757153A (en) * | 2012-07-12 | 2012-10-31 | 山东天兴生物科技有限公司 | Method for treating wastewater generated during production of 12-hydroxy stearic acid |
| CN104445721A (en) * | 2014-11-19 | 2015-03-25 | 南通新邦化工科技有限公司 | Combined treatment method for stearate wastewater |
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Open date: 20090506 |