CN102503014A - Treatment method of glycerin wastewater containing salt - Google Patents
Treatment method of glycerin wastewater containing salt Download PDFInfo
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- CN102503014A CN102503014A CN2011103733373A CN201110373337A CN102503014A CN 102503014 A CN102503014 A CN 102503014A CN 2011103733373 A CN2011103733373 A CN 2011103733373A CN 201110373337 A CN201110373337 A CN 201110373337A CN 102503014 A CN102503014 A CN 102503014A
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Abstract
The invention discloses a treatment method of glycerin wastewater containing salt. Glycerin waste water containing salt produced during different production processes is added in normal butanol with the amount being 1.3 to 3.3 times of wastewater quantity; with the addition of normal butanol, under the normal pressure and the temperature of 30 to 70 DEG C, salt in glycerin wastewater containing salt is separated out by crystallization, the liquid phase is divided into an upper organic phase and a lower water phase; the upper organic phase contains 0.3 percent of salt, and is rectified, normal butanol is recovered, and water is removed at the same time, so that 99.9 percent of pure glycerin serving as a product is obtained; and the lower water phase is filtered, filtrate flows back to an extraction tower for retreatment, and crystallized sodium chloride is washed and recovered. The treatment method has the advantages of simple and convenient process flow, easiness in operation and control, and environmental friendliness; and glycerin and sodium chloride in wastewater can be recycled, so that the production cost can be reduced effectively. The invention is especially suitable for byproducts in epoxide resin production, glycerin byproducts in oil and glycerin chemical production and wastewater treatment of glycerin byproducts in biodiesel production.
Description
Technical field
The present invention relates to a kind of wastewater treatment method, be specifically related to a kind of saliferous glycerine wastewater treatment method.
Background technology
In recent years, along with the growth of epoxy resin and production of biodiesel, the production wastewater treatment amount that contains by-product glycerol sharply rises.Contain a large amount of salts in this glycerine waste water.At present the raw glycerine purifying process will pass through operations such as concentrated, distillation, absorption and IX, could obtain high-quality refining glycerine.Yet, because the salt that contains makes the system elevation of boiling point in the raw glycerine, concentrate and distillation in not only to consume great amount of heat energy, and the salt of separating out along with moisture evaporation deposition causes extra burdens such as operation and equipment loss.Therefore, traditional glycerol purifying technique cost is very high.
Summary of the invention
The object of the present invention is to provide a kind of saliferous glycerine wastewater treatment method; Its technical process is simple, efficient is high, and is little to equipment loss, can reduce the processing cost of saliferous glycerine waste water; And the uniform glycerol product of available quality, thereby can reduce production costs.
The technical solution adopted for the present invention to solve the technical problems is:
The process step of this method is:
1) will be from the propyl carbinol of 1.3 ~ 3.3 times of wastewater flow rates of saliferous glycerine waste water adding that produce in the different production processes;
2) along with the adding of propyl carbinol, at normal pressure, temperature is 30 ~ 70 ℃, and the salt in the saliferous glycerine waste water can be separated out in crystallization, and liquid phase is divided into the organic phase that the upper strata contains 0.3% salt, and lower floor's water;
3) upper organic phase reclaims propyl carbinol through rectifying, removes simultaneously and anhydrates, and obtain 99.9% pure glycerin as product; Lower floor's water filters, and filtrating is back in the extraction tower and handles, crystalline sodium-chlor washing and recycling.
Described upper organic phase is through rectifying; The idiographic flow that reclaims propyl carbinol and pure glycerin is: the upper layer substance stream of extraction tower gets into the first rectification under vacuum tower through first preheater; The first rectification under vacuum tower tower bottoms; Get into the further rectifying separation purification of glycerol of the 3rd rectification under vacuum tower through second preheater, cat head distillates solvent cycle to extraction tower; The first rectification under vacuum column overhead distillates azeotropic liquid; With distillate azeotropic liquid from the second rectification under vacuum column overhead and be mixed into standing demix in the decanting vessel; The decanting vessel upper layer substance flows back to and flows into first rectification under vacuum tower continuation rectifying, and the logistics of decanting vessel lower floor gets into the second rectification under vacuum tower; The second rectification under vacuum Tata stilling goes out the pure water logistics, and cat head distillates azeotropic liquid.
The beneficial effect that the present invention has is:
It is easy that method of the present invention has technical process, easy handling and control, environmental friendliness; Glycerine in the waste water and sodium-chlor all can be recycled, and can effectively reduce production cost.The present invention is specially adapted to the wastewater treatment in epoxy resin production glycerin by-products, oil and fat chemical production glycerin by-products and the production of biodiesel glycerin by-products.
Description of drawings
Accompanying drawing is saliferous glycerine sewage treatment technology process figure.
In the accompanying drawing:
R1, extraction tower, R2, mold, F1, strainer, C1, the first rectification under vacuum tower; C2, the second rectification under vacuum tower, C3, the 3rd rectification under vacuum tower, D1, decanting vessel, H1, first preheater; H2, second preheater, H3, the 3rd preheater, H4, the 4th preheater, H5, pre-cooler; P1, solvent pump, M1, first mixing tank, M2, second mixing tank, M3, the 3rd mixing tank;
1, waste water circulating mixture material, 2, the propyl carbinol recycle stream, 3, the logistics of extraction tower lower floor, 4, the logistics of extraction tower upper strata; 5, mold logistics, 6, filtrating, 7, the sodium chloride crystal logistics, 8, the first rectification under vacuum tower charging; 9, the first rectification under vacuum cat head distillates azeotropic liquid, 10, the first rectification under vacuum tower tower bottoms, the 11, the 3rd rectification under vacuum tower charging, 12, the propyl carbinol returned logistics; 13, glycerol product logistics, 14, two tower azeotrope mixture flow, 15, the logistics of decanting vessel lower floor, 16, the logistics of decanting vessel upper strata; 17, decanting vessel lower floor preheating logistics, 18, the second rectification under vacuum tower charging, 19, the second rectification under vacuum cat head distillates azeotropic liquid, 20, the second rectification under vacuum tower still pure water logistics; 21, propyl carbinol phegma, 22, wastewater feed, 23, waste water, solvent liquid.
Embodiment
Below in conjunction with accompanying drawing and embodiment the present invention is further described.
Shown in accompanying drawing, the process step of this method is:
1) will be from the propyl carbinol of 1.3 ~ 3.3 times of wastewater flow rates of saliferous glycerine waste water adding that produce in the different production processes;
2) along with the adding of propyl carbinol, at normal pressure, temperature is that the salt in the saliferous glycerine waste water can be separated out in crystallization under 30 ~ 70 ℃ the condition, and liquid phase is divided into the organic phase that the upper strata contains 0.3% salt, and lower floor's water;
3) upper organic phase reclaims propyl carbinol through rectifying, removes simultaneously and anhydrates, and obtain 99.9% pure glycerin as product; Lower floor's water filters, and filtrating is back in the extraction tower and handles, crystalline sodium-chlor washing and recycling.
Described upper organic phase is through rectifying; The idiographic flow that reclaims propyl carbinol and pure glycerin is: the upper layer substance stream of extraction tower gets into the first rectification under vacuum tower C1 through the first preheater H1; The first rectification under vacuum tower C1 tower bottoms; Get into the further rectifying separation purification of glycerol of the 3rd rectification under vacuum tower C3 through the second preheater H2, cat head distillates solvent through pump P1 supercharging and pre-cooler H5 cooling, is circulated in the extraction tower R1; The first rectification under vacuum tower C1 cat head distillates azeotropic liquid; With distillate azeotropic liquid from the second rectification under vacuum tower C2 cat head and be mixed into standing demix among the decanting vessel D1; The 3rd preheater H3 preheating of flowing through of decanting vessel D1 upper layer substance passes back into the first rectification under vacuum tower C1 and continues rectifying, and decanting vessel D1 lower floor logistics the 4th preheater H4 preheating gets into the second rectification under vacuum tower C2; The second rectification under vacuum tower C2 tower stilling goes out the pure water logistics, and cat head distillates azeotropic liquid.
The saliferous glycerine waste water that produces during the present invention produces is thick liquid through evaporation concentration, contains 28 ~ 32% glycerine, 50% ~ 54% water, about 18% sodium-chlor and small amount of impurities through analyzing.Waste water circulating mixture material 1 is mixed in the 3rd mixing tank M3 with propyl carbinol recycle stream 2, form waste water, solvent liquid 23 entering extraction tower R1.Operational condition is a normal pressure, and TR is 30 ~ 70 ℃.SX portion water and glycerine get into organic phase, and the sodium-chlor of aqueous phase is owing to the minimizing of water-content is separated out.The water that gets into organic phase can carry the sodium-chlor entering organic phase of trace, and content accounts for 4.8 ~ 5.2 % of total sodium-chlor.Because salts contg is lower in the organic phase, can adopt rectifying to reclaim solvent, extract glycerine.Simultaneously the sodium-chlor of aqueous phase since the increase of solvent and solubleness reduce crystallization and separate out.Therefore utilize the SX crystallization, can avoid or reduce the ebullioscopic influence of salt pair solution.
Through after the extraction tower, mixed solution splits into liquid-liquid-solid three-phase.The upper strata is the organic phase that contains water, glycerine and micro-sodium-chlor.Lower floor is the water that contains little solvent and partial glycerol and sodium-chlor.Solid phase is the sodium chloride crystal of separating out.From extraction tower upper strata logistics 4, reclaim solvent and extract glycerine, extraction tower lower floor logistics 3 process molds form mold logistics 5 backs and feed strainer, and filtrating 6 is back to extraction tower, and gets sodium chloride crystal logistics 7.Solvent recuperation and glycerin extraction be through three vacuum distillation towers, the first rectification under vacuum tower C1, the second rectification under vacuum tower C2, the 3rd rectification under vacuum tower C3, and wherein the first rectification under vacuum tower and the second rectification under vacuum tower constitute the heterogeneous azeotropic rectification system of solvent recuperation.Extraction tower upper strata logistics 4 becomes the first rectification under vacuum tower charging 8 through the first preheater H1 and gets into the first rectification under vacuum tower, working pressure 0.3bar ~ 0.5bar.The first rectification under vacuum tower tower bottoms 10 is propyl carbinol and glycerine mixed solution; Through the second preheater H2 preheating is that the 3rd rectification under vacuum tower charging 11 gets into the 3rd rectification under vacuum tower rectifying; Cat head obtains propyl carbinol returned logistics 12; Through pump P1 supercharging becoming propyl carbinol phegma 21 and be cooled to propyl carbinol recycle stream 2 through pre-cooler and be back to extraction tower, output glycerol product logistics 13 at the bottom of the tower.The first rectification under vacuum cat head distillates azeotropic liquid 9 and is water and propyl carbinol azeotrope, and the mass fraction of water is 0.38.This distillate distillates azeotropic liquid 19 with the second rectification under vacuum cat head to be mixed through the first mixing tank M1, gets into decanting vessel through overcooling.In decanting vessel; Two tower azeotrope mixture flow 14 are layered as decanting vessel lower floor logistics 15 and decanting vessel upper strata logistics 16; Wherein decanting vessel upper strata logistics 16 becomes decanting vessel lower floor preheating logistics 17 through the 3rd preheater H3; Decanting vessel lower floor logistics 15 is preheated to the second rectification under vacuum tower charging 18 through the 4th preheater and gets into the second rectification under vacuum tower, distillates the second rectification under vacuum cat head at cat head and distillates azeotropic liquid 19, and the mass fraction of water is 0.38.The second rectification under vacuum cat head distillates azeotropic liquid 19 backflows and gets into decanting vessel; The output second rectification under vacuum tower still pure water logistics 20 at the bottom of the tower.
Embodiment 1:
This routine propyl carbinol consumption is 2.5 times of factory effluent.Set up flow process according to accompanying drawing, concrete logistics connects the introduction referring to technical process in the summary of the invention.Wastewater feed 22 (flow 1395.2kg/hr, water accounts for 56%, and glycerine accounts for 26%; Sodium-chlor accounts for 18%) with filter F 1 in filtrating 6 (flow 1668.8kg/hr, water accounts for 55%, glycerine accounts for 27%; Sodium-chlor accounts for 15%; Propyl carbinol accounts for 3%) be mixed into waste water circulating mixture material 1 (flow 3064kg/hr), (flow 7500kg/hr) mixes in the 3rd mixing tank M3 with propyl carbinol recycle stream 2, forms waste water, solvent liquid 23 (flow 10564kg/hr) entering extraction tower R1.At normal pressure, temperature is 30 ℃ of operations down.In extractor R1, (flow is 1921.7kg/hr, and water accounts for 55% in output extraction tower lower floor logistics 3; Glycerine accounts for 27%, and sodium-chlor accounts for 15%, and propyl carbinol accounts for 3%) (flow is 8588.29kg/hr with extraction tower upper strata logistics 4; Water accounts for 9.1%; Glycerine accounts for 4.2%, and propyl carbinol accounts for 86.7%), and precipitated sodium chloride crystal 2 52.9kg/hr.
Extraction tower upper strata logistics 4 is heated to 74 ℃ through preheater H1; Form the first rectification under vacuum tower charging 8 and get into the first rectification under vacuum tower C1 at second column plate place; The overhead condenser working pressure is 0.5bar; The first rectification under vacuum cat head distillates azeotropic liquid 9 (flow is 2916.6kg/hr, and water accounts for 38.2%, and propyl carbinol accounts for 61.8%), and (flow is 407.4kg/hr with distillating azeotropic liquid 19 from the second rectification under vacuum cat head of the second rectification under vacuum tower C2; Water accounts for 39.4%, and propyl carbinol accounts for 60.6%) be mixed into two tower azeotrope mixture flow, 14 entering decanting vessel D1 through the first mixing tank M1.14 layerings in D1 of two tower azeotrope mixture flow; Decanting vessel lower floor logistics 15 (flow is 1188.8kg/hr, and water accounts for 79.2%, and propyl carbinol accounts for 20.8%) is heated to 70 ℃ through preheater H4 becomes the second rectification under vacuum tower charging, 18 entering C2; The overhead condenser working pressure is 0.5bar; The second rectification under vacuum cat head distillates azeotropic liquid 19 and returns in the decanting vessel, the second rectification under vacuum tower still pure water logistics, 20 (flow is 781.5kg/hr, and water accounts for 99.99%).Decanting vessel upper strata logistics 16 (flow is 2135.3kg/hr, and water accounts for 15.6%, and propyl carbinol accounts for 84.4%) is heated to 74 ℃ through preheater H3 to be become decanting vessel lower floor preheating logistics 17 and is back among the C1.The first rectification under vacuum tower tower bottoms 10 (flow is 7806.9kg/hr, and glycerine accounts for 4.6%, and propyl carbinol accounts for 95.4%) is heated to 88 ℃ through preheater H2 becomes the 3rd rectification under vacuum tower charging 11 entering the 3rd rectification under vacuum tower C3.The overhead condenser working pressure is 0.3bar.(flow is 7446.1kg/hr to propyl carbinol returned logistics 12; Propyl carbinol purity is 99.99%) be pressurised into propyl carbinol phegma 21 through pump P1; And be cooled to propyl carbinol recycle stream 2 through pre-cooler and return extraction tower R1 recycle; Glycerol product logistics 13 (flow is 360.9kg/hr, and glycerine purity is 99.91%) is product glycerine.The flow of each stream thigh is asked for an interview table 1.
Table
: the propyl carbinol consumption is that 2.5 times of calculation result of wastewater flow rate gather
。
Embodiment 2:
This routine propyl carbinol consumption is 1.3 times of factory effluent.Set up flow process according to accompanying drawing, concrete logistics connects the introduction referring to technical process in the summary of the invention.Wastewater feed 22 (flow 792.1kg/hr, water accounts for 56%, and glycerine accounts for 24%; Sodium-chlor accounts for 20%) with filter F 1 in filtrating 6 (flow 2297.9kg/hr; Water accounts for 55%, and glycerine accounts for 27%, and sodium-chlor accounts for 15%; Propyl carbinol accounts for 3%) be mixed into waste water circulating mixture material 1 (flow 3090kg/hr) and in the 3rd mixing tank M3, mix with propyl carbinol recycle stream 2 (flow 3911.5kg/hr), form waste water, solvent liquid 23 (flow 7010kg/hr) gets into extraction tower R1.At normal pressure, temperature is 50 ℃ of operations down.In extractor R1, (flow is 2443.5kg/hr, and water accounts for 51% in output extraction tower lower floor logistics 3; Glycerine accounts for 25%, and sodium-chlor accounts for 21%, and propyl carbinol accounts for 3%) (flow is 4566.49kg/hr with extraction tower upper strata logistics 4; Water accounts for 10%, and glycerine accounts for 4%, and propyl carbinol accounts for 85.7%; Sodium-chlor accounts for 0.3%), and precipitated sodium chloride crystal 158.6kg/hr.
Extraction tower upper strata logistics 4 is heated to 72 ℃ through preheater H1; Form the first rectification under vacuum tower charging 8 and get into the first rectification under vacuum tower C1 at second column plate place; The overhead condenser working pressure is 0.5bar; The first rectification under vacuum cat head distillates azeotropic liquid 9 (flow is 1577.69kg/hr, and water accounts for 39%, and propyl carbinol accounts for 61%), and (flow is 230.14kg/hr with distillating azeotropic liquid 19 from the second rectification under vacuum cat head of the second rectification under vacuum tower C2; Water accounts for 39%, and propyl carbinol accounts for 61%) be mixed into two tower azeotrope mixture flow, 14 entering decanting vessel D1 through the first mixing tank M1.14 layerings in D1 of two tower azeotrope mixture flow; Decanting vessel lower floor logistics 15 (flow is 671.62kg/hr, and water accounts for 79.2%, and propyl carbinol accounts for 20.8%) is heated to 70 ℃ through preheater H4 becomes the second rectification under vacuum tower charging, 18 entering C2; The overhead condenser working pressure is 0.5bar; The second rectification under vacuum cat head distillates azeotropic liquid 19 and returns in the decanting vessel, the second rectification under vacuum tower still pure water logistics, 20 (flow is 441.48kg/hr, and water accounts for 99.99%).Decanting vessel upper strata logistics 16 (flow is 1136.11kg/hr, and water accounts for 15.6%, and propyl carbinol accounts for 84.4%) is heated to 74 ℃ through preheater H3 to be become decanting vessel lower floor preheating logistics 17 and is back among the C1.The first rectification under vacuum tower tower bottoms 10 (flow is 4111.9kg/hr, and glycerine accounts for 5%, and propyl carbinol accounts for 95%) is heated to 88 ℃ through preheater H2 becomes the 3rd rectification under vacuum tower charging 11 entering the 3rd rectification under vacuum tower C3.The overhead condenser working pressure is 0.3bar.(flow is 3918.1kg/hr to propyl carbinol returned logistics 12; Propyl carbinol purity is 99.99%) be pressurised into propyl carbinol phegma 21 through pump P1; And be cooled to propyl carbinol recycle stream 2 through pre-cooler and return extraction tower R1 recycle; Glycerol product logistics 13 (flow is 192.1kg/hr, and glycerine purity is 99.99%) is product glycerine.The flow of each stream thigh is asked for an interview table 2.
Table 2: the propyl carbinol consumption is that 1.3 times of calculation result of wastewater flow rate gather
Embodiment 3:
This routine propyl carbinol consumption is 3.3 times of factory effluent.Set up flow process according to accompanying drawing, concrete logistics connects the introduction referring to technical process in the summary of the invention.Wastewater feed 22 (flow 1841.9kg/hr, water accounts for 56%, and glycerine accounts for 18%; Sodium-chlor accounts for 26%) with filter F 1 in filtrating 6 (flow 1208.1kg/hr; Water accounts for 55%, and glycerine accounts for 27%, and sodium-chlor accounts for 15%; Propyl carbinol accounts for 3%) be mixed into waste water circulating mixture material 1 (flow 3050kg/hr) and in the 3rd mixing tank M3, mix with propyl carbinol recycle stream 2 (flow 9932.5kg/hr), form waste water, solvent liquid 23 (flow 13010kg/hr) gets into extraction tower R1.At normal pressure, temperature is 70 ℃ of operations down.In extractor R1, (flow is 1533.0kg/hr, and water accounts for 43% in output extraction tower lower floor logistics 3; Glycerine accounts for 21%, and sodium-chlor accounts for 33%, and propyl carbinol accounts for 3%) (flow is 11512kg/hr with extraction tower upper strata logistics 4; Water accounts for 9%, and glycerine accounts for 4%, and propyl carbinol accounts for 86.7%; Sodium-chlor accounts for 0.3%), and precipitated sodium chloride crystal 3 24.9kg/hr.
Extraction tower upper strata logistics 4 is heated to 74 ℃ through preheater H1; Form the first rectification under vacuum tower charging 8 and get into the first rectification under vacuum tower C1 at second column plate place; The overhead condenser working pressure is 0.5bar; The first rectification under vacuum cat head distillates azeotropic liquid 9 (flow is 3887.8kg/hr, and water accounts for 38%, and propyl carbinol accounts for 62%), and (flow is 540.6kg/hr with distillating azeotropic liquid 19 from the second rectification under vacuum cat head of the second rectification under vacuum tower C2; Water accounts for 39%, and propyl carbinol accounts for 61%) be mixed into two tower azeotrope mixture flow, 14 entering decanting vessel D1 through the first mixing tank M1.14 layerings in D1 of two tower azeotrope mixture flow; Decanting vessel lower floor logistics 15 (flow is 1577.5kg/hr, and water accounts for 79.2%, and propyl carbinol accounts for 20.8%) is heated to 70 ℃ through preheater H4 becomes the second rectification under vacuum tower charging, 18 entering C2; The overhead condenser working pressure is 0.5bar; The second rectification under vacuum cat head distillates azeotropic liquid 19 and returns in the decanting vessel, the second rectification under vacuum tower still pure water logistics, 20 (flow is 1037kg/hr, and water accounts for 99.99%).Decanting vessel upper strata logistics 16 (flow is 2580.75kg/hr, and water accounts for 15.6%, and propyl carbinol accounts for 84.4%) is heated to 74 ℃ through preheater H3 to be become decanting vessel lower floor preheating logistics 17 and is back among the C1.The first rectification under vacuum tower tower bottoms 10 (flow is 10439.94kg/hr, and glycerine accounts for 5%, and propyl carbinol accounts for 95%) is heated to 88 ℃ through preheater H2 becomes the 3rd rectification under vacuum tower charging 11 entering the 3rd rectification under vacuum tower C3.The overhead condenser working pressure is 0.3bar.(flow is 9952.45kg/hr to propyl carbinol returned logistics 12; Propyl carbinol purity is 99.99%) be pressurised into propyl carbinol phegma 21 through pump P1; And be cooled to propyl carbinol recycle stream 2 through pre-cooler and return extraction tower R1 recycle; Glycerol product logistics 13 (flow is 487.5kg/hr, and glycerine purity is 99.99%) is product glycerine.The flow of each stream thigh is asked for an interview table 3.
Table 3: the propyl carbinol consumption is that 3.3 times of calculation result of wastewater flow rate gather
Claims (2)
1. saliferous glycerine wastewater treatment method is characterized in that the process step of this method is:
1) will be from the propyl carbinol of 1.3 ~ 3.3 times of wastewater flow rates of saliferous glycerine waste water adding that produce in the different production processes;
2) along with the adding of propyl carbinol, at normal pressure, temperature is 30 ~ 70 ℃, and the salt in the saliferous glycerine waste water can be separated out in crystallization, and liquid phase is divided into the organic phase that the upper strata contains 0.3% salt, and lower floor's water;
3) upper organic phase reclaims propyl carbinol through rectifying, removes simultaneously and anhydrates, and obtain 99.9% pure glycerin as product; Lower floor's water filters, and filtrating is back in the extraction tower and handles, crystalline sodium-chlor washing and recycling.
2. a kind of saliferous glycerine wastewater treatment method according to claim 1; It is characterized in that: described upper organic phase is through rectifying; The idiographic flow that reclaims propyl carbinol and pure glycerin is: the upper layer substance stream of extraction tower (R1) gets into the first rectification under vacuum tower (C1) through first preheater (H1); First rectification under vacuum tower (C1) tower bottoms; Get into further rectifying separation purification of glycerol of the 3rd rectification under vacuum tower (C3) through second preheater (H2), cat head distillates in solvent cycle to the extraction tower (R1); First rectification under vacuum tower (C1) cat head distillates azeotropic liquid; With distillate azeotropic liquid from second rectification under vacuum tower (C2) cat head and be mixed into standing demix in the decanting vessel (D1); Decanting vessel (D1) upper layer substance flows back to and flows into the first rectification under vacuum tower (C1) continuation rectifying, and the logistics of decanting vessel (D1) lower floor gets into the second rectification under vacuum tower (C2); Second rectification under vacuum tower (C2) the tower stilling goes out the pure water logistics, and cat head distillates azeotropic liquid.
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| CN102887604A (en) * | 2012-10-29 | 2013-01-23 | 杭州油脂化工有限公司 | Method for hydrolyzing sweet water through processing grease by using dissolved air flotation |
| CN104291523A (en) * | 2014-09-18 | 2015-01-21 | 波鹰(厦门)科技有限公司 | Method for recovering sodium chloride and glycerin from glycerin-containing high-salinity organic wastewater |
| CN104326872A (en) * | 2014-10-11 | 2015-02-04 | 波鹰(厦门)科技有限公司 | Method for recycling glycerol in organic wastewater with high salt content |
| WO2017001892A1 (en) | 2015-06-29 | 2017-01-05 | Sapec Química, Sa. | Crude glycerol purification process |
| CN107324577A (en) * | 2017-08-17 | 2017-11-07 | 长兴上拓环境科技有限公司 | A kind of epoxy resin production waste-water recycling treatment process |
| CN108298752A (en) * | 2018-01-17 | 2018-07-20 | 北京凯瑞英科技有限公司 | A kind of highly salt containing organic waste water processing system and the method for handling waste water |
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| US10364162B2 (en) | 2017-06-30 | 2019-07-30 | National Tsing Hua University | System and method for treating salt-containing glycerin wastewater |
| CN110229046A (en) * | 2018-03-05 | 2019-09-13 | 南通星辰合成材料有限公司 | A kind of device and method extracting glycerol and class glyceryl alcohol from epoxy wastewater evaporation mother liquor |
| CN110776030A (en) * | 2019-11-01 | 2020-02-11 | 西安交通大学 | Crystallization system for extracting NaCl aqueous solution by butanol injection flash evaporation and working method |
| CN115612559A (en) * | 2022-08-24 | 2023-01-17 | 东莞市新东欣环保投资有限公司 | Treatment method of glycerin residue |
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| CN85109000A (en) * | 1984-12-10 | 1986-07-09 | 国际壳牌研究有限公司 | From brine waste, reclaim glycerine |
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| CN102887604B (en) * | 2012-10-29 | 2014-01-01 | 杭州油脂化工有限公司 | Method for hydrolyzing sweet water through processing grease by using dissolved air flotation |
| CN102887604A (en) * | 2012-10-29 | 2013-01-23 | 杭州油脂化工有限公司 | Method for hydrolyzing sweet water through processing grease by using dissolved air flotation |
| CN104291523A (en) * | 2014-09-18 | 2015-01-21 | 波鹰(厦门)科技有限公司 | Method for recovering sodium chloride and glycerin from glycerin-containing high-salinity organic wastewater |
| CN104326872A (en) * | 2014-10-11 | 2015-02-04 | 波鹰(厦门)科技有限公司 | Method for recycling glycerol in organic wastewater with high salt content |
| CN104326872B (en) * | 2014-10-11 | 2016-06-08 | 波鹰(厦门)科技有限公司 | The recovery method of glycerol in highly salt containing organic waste water |
| WO2017001892A1 (en) | 2015-06-29 | 2017-01-05 | Sapec Química, Sa. | Crude glycerol purification process |
| US10364162B2 (en) | 2017-06-30 | 2019-07-30 | National Tsing Hua University | System and method for treating salt-containing glycerin wastewater |
| CN107324577A (en) * | 2017-08-17 | 2017-11-07 | 长兴上拓环境科技有限公司 | A kind of epoxy resin production waste-water recycling treatment process |
| CN108298752B (en) * | 2018-01-17 | 2021-06-01 | 北京凯瑞英科技有限公司 | High-salt-content organic wastewater treatment system and wastewater treatment method |
| CN108298752A (en) * | 2018-01-17 | 2018-07-20 | 北京凯瑞英科技有限公司 | A kind of highly salt containing organic waste water processing system and the method for handling waste water |
| CN110229046B (en) * | 2018-03-05 | 2023-07-28 | 南通星辰合成材料有限公司 | Device and method for extracting glycerol and glycerol-like alcohol from epoxy wastewater evaporation mother liquor |
| CN110229046A (en) * | 2018-03-05 | 2019-09-13 | 南通星辰合成材料有限公司 | A kind of device and method extracting glycerol and class glyceryl alcohol from epoxy wastewater evaporation mother liquor |
| CN109574801A (en) * | 2018-11-13 | 2019-04-05 | 南通新邦化工科技有限公司 | A kind of glycerol recovery process |
| CN109824191A (en) * | 2018-12-12 | 2019-05-31 | 张家港衡业特种树脂有限公司 | Glycerol is extracted in haline water in epoxy resin production process |
| CN110776030A (en) * | 2019-11-01 | 2020-02-11 | 西安交通大学 | Crystallization system for extracting NaCl aqueous solution by butanol injection flash evaporation and working method |
| CN115612559A (en) * | 2022-08-24 | 2023-01-17 | 东莞市新东欣环保投资有限公司 | Treatment method of glycerin residue |
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