CN1161316C - Lactic acid refining short range distillation process with drum evaporator - Google Patents
Lactic acid refining short range distillation process with drum evaporator Download PDFInfo
- Publication number
- CN1161316C CN1161316C CNB011280417A CN01128041A CN1161316C CN 1161316 C CN1161316 C CN 1161316C CN B011280417 A CNB011280417 A CN B011280417A CN 01128041 A CN01128041 A CN 01128041A CN 1161316 C CN1161316 C CN 1161316C
- Authority
- CN
- China
- Prior art keywords
- lactic acid
- short
- distillation
- drum evaporator
- vapor pressure
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The present invention relates to a method for refining lactic acid by short-range distillation and a rotating drum evaporator, which belongs to the technique for purifying organic compounds. The method comprises the procedures that 1, industrial grade coarse lactic acid after decolorization and calcium sulfate removal is conveyed to a short-range distiller, and the industrial grade coarse lactic acid is continuously fed in for distillation dewatering at certain vapor pressure, vacuum degree and heating temperature; b, concentrated lactic acid from the short-range distiller is conveyed into the rotating drum evaporator, feeding, evaporation and deslagging are simultaneously carried out at certain vapor pressure, vacuum degree and heating temperature, and meanwhile, colorless lactic acid finished products which accord with standards are obtained. The prevent invention adopts a molecular distillation technique and is especially suitable for producing refining L-lactic acid.
Description
The present invention relates to a kind of method with short-path distillation and drum evaporator fine purification of lactic acid, the purification techniques that belongs to organic compound, be applicable to the technical grade crude lactic acid (comprise D---lactic acid, L---lactic acid and DL---lactic acid) direct purification, make it finished product lactic acid water white transparency, the thermostability height, meet or exceed corresponding national standards.
Lactic acid is a kind of fine chemical product of food chemical industry class, its preparation technology is for being main raw material with corn or potato starch, lime carbonate, add microbial strains, obtain calcium lactate liquid through liquid fermenting and filtration, again through concentrate, operation such as acidolysis handles, separate obtaining the technical grade crude lactic acid behind the elimination calcium sulfate, with the method for physics or chemistry the technical grade crude lactic acid is made with extra care purification at last, obtain finished product lactic acid.In the prior art, a lot of to the process for purification of technical grade crude lactic acid, for example calcium lactate crystallization process, esterification process, extraction process, ion-exchange activated carbon decolorizing method and distillation method or the like, wherein, the crystallization process complex steps; Esterification process and extraction process are introduced organic solvent, are unsuitable for food, pharmaceutical grade lactic acid-producing; Ion-exchange activated carbon decolorizing method is in preparation, the regeneration existing problems of separating agent; Distillation method is that physical purification method, especially short-path distillation and molecular distillation are the novel distillation techniques that occurs in recent years, at present, and the industrial distillation plant of existing moulding on the market, and comprising that vitamin-E, oil and fat chemical industry are applied.The Chinese invention patent application discloses a kind of short-path molecular distillation technology of lactic acid for No. 00114432.4, promptly lactic acid or the low levels lactic acid work in-process with food grade or pharmaceutical grade are raw material, adopt the thermal distillation that adds of high vacuum state, at first will be that 30～80% lactic acid solution is sent into vaporizer through the lactic acid content of ion-exchange, keep quantitative and operating pressure, the limit adds thermal distillation, the limit distillates moisture content, cooling is collected, lactic acid content is remained on more than 95%, again spissated lactic acid is sent in the short-range molecular distillation vaporizer, keep a certain amount of and operating pressure, between 60～115 ℃ of temperature of charge, add thermal distillation, when temperature of charge is higher than 115 ℃, feed a small amount of water vapor, to slow down the acid by dehydrating lactic auto-polymerization, when temperature of charge rises to 120 ℃, stop distillation, at last the lactic acid that makes is carried out content and be adjusted to 88～90%, promptly obtain fine purification of lactic acid.Though this technology is introduced lactic acid purification field with the short-path distillation technology, but also exist not enough: at first, this technology system is a raw material with the lactic acid of food grade or pharmaceutical grade, and need to do pre-treatment through ion exchange column earlier, and in practice, after lactic acid content reaches certain value (for example greater than 50%), can't pass through ion exchange column: secondly, the selected short-path distillation vacuum tightness of this technology is 100～1000pa, be higher than the vacuum tightness of classical short-path distillation far away, the choosing value of the vacuum tightness of general short-path molecular distillation technology is between 0.1～100pa.Too high vacuum tightness choosing value, hyper acid for the polygalacto of generation, can influence the raising of the lactic acid rate of recovery; At last, this technology need have external condenser and cold-trap supporting, has increased facility investment, and it is the circulation distillation that short-distance distiller adopts, and makes lactic acid evaporation quality instability easily, thereby causes the raising of production cost.
The objective of the invention is to overcome the above-mentioned deficiency of prior art, develop a kind of short-path distillation modern technique that both adopted, can simplify process for refining again, improve the lactic acid quality, can also cut down the consumption of energy, improve the method for purification of yield, the theory of this method utilization molecular distillation, short-distance distiller and drum evaporator are organically combined, finish refining extraction to the technical grade crude lactic acid, finished product lactic acid after the purification is colourless, and quality is reached the standard of Japan, U.S.'s like product, and can produce crystalline lactic acid.
This method with short-path distillation and drum evaporator fine purification of lactic acid that the present invention provides mainly contains operations such as adopting the dehydration of physics method, molecular distillation, includes following steps;
A. will decolour and remove the technical grade crude lactic acid (lactic acid content is 20～30%) of calcium sulfate, be delivered to dehydration in the short-distance distiller, under the condition of 60～70 ℃ of vapor pressure 0.02～0.05Mpa, vacuum tightness 0.80～0.97Mpa, material Heating temperatures, the continuously feeding distillation dehydration, and the lactic acid after will concentrating is delivered to drum evaporator continuously;
B. the lactic acid (lactic acid content is 70～80%) after will concentrating from short-distance distiller, be delivered to and carry out molecular distillation in the drum evaporator, at vapor pressure 0.02～0.05Mpa, vacuum tightness 1～30pa, under the condition that the material Heating temperature is 50～70 ℃, limit charging evaporation, the limit deslagging obtains meeting the colourless finished product lactic acid of national standard simultaneously.
Because the technical grade crude lactic acid contains organic impurity such as thalline degradation product and yellowly; refining colourless finished product lactic acid; must remove color earlier; the present invention removes look with gac before making it to enter the short-distance distiller dehydration; certainly, also can after the dehydration of technical grade crude lactic acid, remove look with gac again, in a word; gac removes the ordering of look operation, does not influence the claimed flesh and blood of the present invention.
Compared with prior art, the present invention mainly adopts the operational path of low temperature, condition of high vacuum degree and rotary drum tower evaporation, has following characteristics:
1. the present invention adopts pure physical method, need not enter yin, yang ion exchange resin exchange column, thereby saves the acid-alkali treatment step, reduces the pollution of acid base pair environment, and has reduced the loss of facility investment and acid-base raw materials and the loss of lactic acid.
2. the condition of high vacuum degree numerical value selected for use of the present invention is 1～30pa, and this interval polymerization lactic acid that generates is less than 2%, and therefore, the lactic acid rate of recovery can reach between 80～85%, and between 100～1000pa that prior art is selected for use, generates polymerization lactic acid considerably beyond this number.
3. the present invention adopts short distiller and drum evaporator combination, and is lower than simple employing short-distance distiller power consumption, generally saves 0.4～0.6 ton of steam/finished product.
4. the present invention adopts serialization production, and up-to-standard rate is 100%, and prior art adopts the circulation distillation with short distance, and it is more generally to generate polymerization lactic acid, and the finished product lactic acid quality of output is also unstable.
In order more clearly to sketch the present invention, it is as follows to enumerate embodiment, but illustrated embodiment does not have any restriction to the claimed content of the present invention.
Embodiment
At first will remove by filter the thick L of technical grade---the lactic acid of solvable calcium sulfate through acidolysis, with behind the activated carbon decolorizing with pump delivery to vacuum receiver, the feed liquid after the vacuum outgas under under meter control, with 2 tons/time flow velocity to enter the first cover evaporation area be 14M
2Short-distance distiller in the dehydration, at vapor pressure 0.02～0.05Mpa, vacuum tightness 800～970pa, 60～70 ℃ of conditions of material Heating temperature property distillation dehydration next time, back L---lactic acid concn 60～70% obtains dewatering, L after the dehydration---lactic acid under under meter control with 1.3 tons/time flow velocity enter the second cover short-distance distiller of series combination with it, the evaporation area of this distiller is 8M
2, under identical technical qualification, further dewater and collect middle distillate, further after the dehydration L---lactic acid content is greater than 80%, and the middle distillate of collection is 60～80%.L---lactic acid after concentrating by second short-distance distiller, under under meter control, with 1.0 tons/time flow velocity to enter evaporation area be 46M
2Drum evaporator carry out molecular distillation, at vacuum tightness 1～30pa, vapor pressure 0.02～0.05Mpa, material Heating temperature 50---carry out essence under 70 ℃ of conditions and steam, water white transparency finished product L---the lactic acid that meets national standard is collected on limit charging evaporation, limit deslagging, limit.Can reach Japan, U.S.'s industry standard according to the testing product quality, L---the lactic acid rate of recovery surpasses 75% level of developed country, has reached 80～85%.The experimental data that following table provides for embodiment.
| Numbering | Technical grade L-lactic acid concn %) | The dehydration of first short-distance distiller | Second short-distance distiller slightly steams | The drum evaporator distillation | Finished product L-lactic acid | |||||||||||
| Flow velocity T/time | Vapor pressure Mp a | Vacuum tightness pa | Temperature of charge ℃ | Flow velocity T/ h | Vapor pressure MP a | Vacuum tightness pa | Temperature of charge ℃ | Flow velocity T/h | Vapor pressure Mp a | Vacuum tightness pa | Distillation temperature ℃ | Concentration content % | Color | Rate of recovery % | ||
| 1 | 20 | 2 | 0.03 | 750 | 80 | 1.3 | 0.05 | 970 | 70 | 1 | 0.02 | 10 | 55 | 91.56 | Water white transparency | 84 .8 |
| 2 | 20 | 2 | 0.04 | 750 | 85 | 1.3 | 0. 05 | 970 | 70 | 1 | 0.03 | 20 | 65 | 95.68 | Water white transparency | 81 .5 |
| 3 | 25 | 2 | 0.03 | 750 | 80 | 1.3 | 0. 05 | 970 | 70 | 1 | 0.02 | 10 | 55 | 96.1 | Water white transparency | 81 |
| 4 | 25 | 2 | 0.04 | 750 | 85 | 1.3 | 0. 05 | 970 | 70 | 1 | 0.03 | 20 | 65 | 96.3 | Water white transparency | 80 |
| 5 | 30 | 2 | 0.03 | 750 | 80 | 1.3 | 0. 05 | 970 | 70 | 1 | 0.02 | 10 | 55 | 93.2 | Water white transparency | 83 |
| 6 | 30 | 2 | 0.04 | 750 | 85 | 1.3 | 0. 05 | 970 | 70 | 1 | 0.03 | 20 | 65 | 96.83 | Water white transparency | 80 |
Claims (2)
1, with the method for short-path distillation and drum evaporator fine purification of lactic acid, mainly contain and adopt the dehydration of physics method, molecular distillation purification process, it is characterized in that may further comprise the steps:
A, will decolour and remove calcium sulfate and lactic acid concn content is the technical grade crude lactic acid of 20-30%, be delivered in the placed in-line two cover short-distance distillers, at vapor pressure 0.02-0.05MPa, vacuum tightness 0.80-0.97MPa, under Heating temperature 60-70 ℃ the condition, the lactic acid after the continuously feeding distillation dehydration also will concentrate is delivered to drum evaporator continuously:
B, will concentrate the back and lactic acid concn content be the lactic acid of 70-80% from short-distance distiller, be delivered in the drum evaporator, at vapor pressure 0.02-0.05MPa, vacuum tightness 1-30Pa,, under Heating temperature 50-70 ℃ the condition, limit charging evaporation, the limit deslagging obtains meeting the colourless finished product lactic acid that Huaihe River is marked by country simultaneously.
2, the method with short-path distillation and drum evaporator fine purification of lactic acid according to claim 1 is characterized in that technical grade crude lactic acid used in a step is a L-lactic acid.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB011280417A CN1161316C (en) | 2001-08-15 | 2001-08-15 | Lactic acid refining short range distillation process with drum evaporator |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB011280417A CN1161316C (en) | 2001-08-15 | 2001-08-15 | Lactic acid refining short range distillation process with drum evaporator |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1335294A CN1335294A (en) | 2002-02-13 |
| CN1161316C true CN1161316C (en) | 2004-08-11 |
Family
ID=4667939
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB011280417A Expired - Fee Related CN1161316C (en) | 2001-08-15 | 2001-08-15 | Lactic acid refining short range distillation process with drum evaporator |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1161316C (en) |
Families Citing this family (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP2401066B1 (en) | 2009-02-25 | 2017-10-25 | Council of Scientific & Industrial Research | A polybenzimidazole based premembrane for deacidification; a process for the preparation of the membrane from the premembrane and a process of deacidification |
| CN106422383B (en) * | 2016-10-10 | 2019-02-15 | 肇庆市和邦机械制造有限公司 | A kind of short-path evaporator |
| CN107098808B (en) * | 2017-05-05 | 2020-01-31 | 湖北壮美生物科技有限公司 | Preparation method and production device of high-purity high-content normal-temperature non-crystallized lactic acid products |
| CN109265338A (en) * | 2018-10-09 | 2019-01-25 | 武汉三江航天固德生物科技有限公司 | The production method of medical sodium lactate solution |
| CN111777504B (en) * | 2020-08-11 | 2021-03-19 | 上海汉禾生物新材料科技有限公司 | Method for purifying L-lactic acid extracted from fermentation liquor |
| CN113461515B (en) * | 2021-07-16 | 2024-02-06 | 颐中（青岛）实业有限公司 | Lactic acid refining extraction process and application thereof |
| CN115737548A (en) * | 2022-11-21 | 2023-03-07 | 四川汇宇制药股份有限公司 | Preparation method of famotidine injection |
-
2001
- 2001-08-15 CN CNB011280417A patent/CN1161316C/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| CN1335294A (en) | 2002-02-13 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US6043392A (en) | Method for conversion of biomass to chemicals and fuels | |
| CN103408086A (en) | MVR (Mechanical Vapor Recompression) vapor-stripping deamination system and application method thereof | |
| CN101654305B (en) | Process for changing phenolic nitrate effluent into useful material by extracting, evaporating, crystallizing and coupling | |
| CN102165033A (en) | Methods and systems for preparing materials for sucralose production | |
| CN104445276A (en) | Method for efficiently preparing monocyanamide solution | |
| EP0029536A1 (en) | Process for removing and recovering ammonia from aqueous liquors | |
| CN101007756A (en) | Technical process of preparing high-purity L-lactic acid | |
| CN101182079B (en) | Citric acid mother liquor treatment process | |
| CN102952831A (en) | Manufacturing process of purified lactic acid | |
| CN102260163B (en) | Method for recovering lactic acid from marigold fermentation wastewater | |
| CN1161316C (en) | Lactic acid refining short range distillation process with drum evaporator | |
| CN112939387A (en) | Calcium nitrate coupled sludge thermokalite hydrolysis treatment method and system | |
| CN100374405C (en) | Process for preparing calcium formate from recovered formylic acid in waste water of epoxy soybean oil | |
| CN102993028B (en) | Purifying method of dimethyl diallyl ammonium chloride monomer | |
| CN101234960A (en) | Method for preparing high-pure lactic acid by using centrifugal molecular distillation technique | |
| CN114671405A (en) | Process for preparing high-purity hydrogen chloride from by-product hydrochloric acid in methane chloride process | |
| CN101704843A (en) | Glyphosate continuous desolventizing production process | |
| CN103213953B (en) | A kind of technique being extracted ammonium thiosulfate, ammonium thiocyanate by desulfurization waste liquor | |
| CN1412107A (en) | Production method of potassium dihydrogen phosphate | |
| CN111186848A (en) | Process and device for refining byproduct ammonium sulfate in isophthalonitrile production | |
| JP2004067922A (en) | Process for treating de-ammoniacal liquor | |
| CN108503532A (en) | A kind of processing method for the by-product tail gas preparing Zassol | |
| CN221662613U (en) | System for sodium sulfate waste salt is handled in cooperation with resourceful treatment | |
| CN1083826C (en) | One-step lactic acid purification process for preparing high-purity heat-stable lactic acid and apparatus thereof | |
| CN1193469A (en) | Method for directly producing concentrated fodder from fermented liquid of citric acid |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C06 | Publication | ||
| PB01 | Publication | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| DD01 | Delivery of document by public notice |
Addressee: Li Xiangpu Document name: Notification of Termination of Patent Right |
|
| C17 | Cessation of patent right | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20040811 Termination date: 20090815 |