CN102517346A - Method for preparing L-lactic acid and/or L-lactate - Google Patents
Method for preparing L-lactic acid and/or L-lactate Download PDFInfo
- Publication number
- CN102517346A CN102517346A CN2011104215846A CN201110421584A CN102517346A CN 102517346 A CN102517346 A CN 102517346A CN 2011104215846 A CN2011104215846 A CN 2011104215846A CN 201110421584 A CN201110421584 A CN 201110421584A CN 102517346 A CN102517346 A CN 102517346A
- Authority
- CN
- China
- Prior art keywords
- lactic acid
- acidolysis
- liquid
- fermentation
- carried out
- 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.)
- Pending
Links
Landscapes
- Preparation Of Compounds By Using Micro-Organisms (AREA)
Abstract
The invention discloses a method for preparing L-lactic acid and/or L-lactate. The method sequentially comprises the following steps of: a) preparing an L-lactic acid fermentation solution by microbial fermentation; b) treating the L-lactic acid fermentation solution by adopting any one of flocculation, filtration, centrifuging and ultra-filtration to obtain a clear fermentation solution; c) performing acidolysis and filtration on the clear fermentation solution to obtain acidolysis filtrate; d) decolorizing the acidolysis filtrate to obtain a decolorized solution; and e) separating the decolorized solution by adopting anion adsorption exchange resin, and thus obtaining the L-lactic acid and/or the L-lactate. By adopting the technical scheme, the method only has five steps, and a nano membrane filtration step and a molecular distillation step are not used any more, so compared with the conventional method, the method has the advantages of a few steps, low equipment purchasing cost and using cost, low energy consumption and easily controlled production cost. By adopting the method, the manufacturing cost of the L-lactic acid and/or the L-lactate is low.
Description
Technical field
The present invention relates to a kind of L-lactic acid and/or the Lactated preparation method of L-.
Background technology
Lactic acid is important biochemical industry product, is widely used in fields such as medicine, food, daily use chemicals, chemical industry, oil, leather.Utilize the L-lactic acid polymerizes to produce the biodegradable material POLYACTIC ACID in recent years in the world, and development rapidly, the degradability that POLYACTIC ACID is excellent, the great development prospect of having showed L-lactic acid to the world.L-Sodium.alpha.-hydroxypropionate/potassium is applicable in the meat product, because their pH value is for neutrality and have a little saline taste, freshening effect is remarkable, and L-Sodium.alpha.-hydroxypropionate/potassium is widely used in the products such as sausage, ham, poultry as fungistat.
At present, the method for from the L-lactic acid fermentation liquid, extracting L-lactic acid mainly is a calcium salt method, that is: in above-mentioned fermented liquid, add the vitriol oil and carry out acidolysis, with generation calcium sulfate precipitation and crude lactic acid, and removes by filter calcium sulfate precipitation; Crude lactic acid again through activated carbon decolorizing, de-ionized processing, nanofiltration, concentrate, extraction step behind the short-path distillation etc., to process technical grade and food grade L-lactic acid.The employed ceramic membrane of the membrane filtration of receiving, organic membrane, metallic membrane cost an arm and a leg, and work-ing life is short, film are returned to wash when handling produce great amount of wastewater, and the processing cost of waste water is higher; The energy consumption of short-path distillation is high.The production of L-Sodium.alpha.-hydroxypropionate/potassium mostly adopts sodium hydroxide/Pottasium Hydroxide and refining L-lactic acid direct reaction to make.This makes the process step of existing method many, equipment purchasing cost and use cost height, energy consumption is high, production cost is wayward, so that L-lactic acid and/or the Lactated manufacturing cost of L-are higher.
Summary of the invention
Technical problem to be solved by this invention provides a kind of L-lactic acid and/or the Lactated preparation method of L-, adopts present method, and the Lactated manufacturing cost of L-lactic acid and/or L-is lower.
For solving the problems of the technologies described above, the invention provides a kind of L-lactic acid and/or the Lactated preparation method of L-, comprise following process step successively:
A) prepare the L-lactic acid fermentation liquid through microbial fermentation;
B) adopt any method in flocculation and filtration, centrifugal, the ultrafiltration, the L-lactic acid fermentation liquid handled, fermentation clear liquid;
C) fermentation clear liquid is carried out acidolysis, filtration treatment, get the acidolysis cleaner liquid;
D) to the processing of decolouring of acidolysis cleaner liquid, destainer;
E) adopt negatively charged ion absorption exchange resin that destainer is separated, make L-lactic acid and/or L-lactic acid salt.
For can concise description for the purpose of the problem, below L-lactic acid according to the invention and/or the Lactated preparation method of L-be all abbreviated as present method.
After adopting above technical scheme; Present method only has five process steps, does not re-use to receive membrane filtration, these two process steps of short-path distillation, like this; Compare with existing method, the process step of present method is few, the equipment purchasing cost and use cost is low, energy consumption is low, production cost be easy to control.Therefore, adopt present method, the Lactated manufacturing cost of L-lactic acid and/or L-is lower.
In present method:
A) the L-lactic acid fermentation liquid in the step is to be carbon source with starch, glucose, fructose, beet sugar or its molasses; Arbitrary strain fermentation through in Lactobacillus amylophilus, lactobacterium casei, bacillus acidocldarius or the Rhizopus oryzae makes; Flow in real time in the fermenting process and add pH regulator agent adjusting pH value; The weight percent concentration of pH regulator agent is 20-30%, and described pH regulator agent is lime carbonate or calcium hydroxide, makes the L-lactic acid fermentation liquid that L-lactic acid ca concentration is 100-200g/L.
B) first pH with the L-lactic acid fermentation liquid is transferred to 9.0-11.0 in the step, adopts alkaline flocculation agent that this L-lactic acid fermentation liquid is handled again, and flocculation temperature is 90-95 ℃; Or b) whizzer of employing rotating speed 3000-6000rpm in the step is handled the L-lactic acid fermentation liquid; Or b) ultra-filtration membrane of employing molecular weight cut-off 1000-20000D in the step is handled the L-lactic acid fermentation liquid.To remove biomass, protein, thalline, part polysaccharide and other macromolecular substance.
C) in the step fermentation clear liquid being carried out the condition that acidolysis handles is: temperature 85-95 ℃, pressure-controlling is at 0.01-0.5bar; Acidolysis finished when c) acid hydrolysis solution pH was 1.5-2.5 in the step, and acid hydrolysis solution is carried out filtration treatment, and getting the L-lactic acid concn is the acidolysis cleaner liquid of 100-200g/L.Present method adopts the low pressure acidolysis, in acidolysis, acid hydrolysis solution is concentrated and remove the volatilizable thing of part low pressure.
D) in the step to the acidolysis cleaner liquid condition of handling of decolouring be: make the acidolysis cleaner liquid cross the decolouring of carbon post with the flow velocity of 0.5-3.0BV/h, the gac that loads in the carbon post is any among gac GH-15, the gac GX830.In the time of decolouring, can remove the organic macromolecules such as protein in the acidolysis cleaner liquid.
E) let destainer with the flow velocity of the 0.5-2.0BV/h negatively charged ion absorption exchange resin of flowing through in the step; When reaching absorption exchange when saturated; As eluent said resin is carried out wash-out with mineral acid, get L-lactic acid, as eluent said resin is carried out wash-out with mineral alkali or inorganic salt; Get corresponding L-lactic acid salt; The concentration of eluent is controlled at 0.05-2.0N, flow rate control at 0.5-3.0BV/h, and described negatively charged ion absorption exchange resin is for having the negatively charged ion absorption exchange resin of selecting exchangeability to L-lactic acid, and described mineral acid is any in sulfuric acid, hydrochloric acid, the nitric acid; Described mineral alkali is any in sodium hydroxide, Pottasium Hydroxide, the ammoniacal liquor, and described inorganic salt are any in Repone K, sodium sulfate, SODIUMNITRATE, sodium phosphate, vitriolate of tartar, the potassiumphosphate.When destainer was flowed through negatively charged ion absorption exchange resin, the alkaline reactive group on lactate ion that destainer is contained and the negatively charged ion absorption exchange resin adsorbed exchange.
Described negatively charged ion absorption exchange resin can be following resin and their mixture:
The product grade name type
D201 vinylbenzene macropore highly basic
D202 vinylbenzene macropore highly basic
D301 vinylbenzene macropore weak base
700 vinylbenzene macropore weak base
More than the equal buyable of listed various negatively charged ion absorption exchange resins, and L-lactic acid all had absorption, exchange force.Need to prove, at the e of present method) in the step, described negatively charged ion absorption exchange resin is not limit by the above rosin products title and the trade mark of listing.
Embodiment
Below can further be well understood to the present invention through embodiment given below.But they are not to qualification of the present invention.
Embodiment 1:
The preparation method of L-lactic acid and L-Sodium.alpha.-hydroxypropionate comprises following process step successively:
A) prepare the L-lactic acid fermentation liquid through microbial fermentation:
The bacillus acidocldarius that the used bacterial classification that ferments is known in the art; Ferment used seed culture medium and preparation thereof, fermention medium prescription and be prepared as the prior art part; Here repeating no more, in the fermention medium is that the glucose of 200g/ L is that carbon source, yeast powder are that nitrogenous source ferments with concentration; Leavening temperature is 50-52 ℃; Flow in real time in the fermenting process and add pH regulator agent adjusting pH value; Making pH is 6.0-6.2; The pH regulator agent concentration that is weight percentage is 20% calcium hydroxide, when glucose has consumed, during fermentation ends, make 2700ml, L-lactic acid ca concentration is the L-lactic acid fermentation liquid of 159g/L.Through the glucose concn in the adjusting fermention medium and the concentration of pH regulator agent, the concentration of coming corresponding adjusting fermented product.
B) to the L-lactic acid fermentation liquid flocculate, filtration treatment, fermentation clear liquid:
Getting the L-lactic acid ca concentration that a) step makes is the L-lactic acid fermentation liquid 2700ml of 159g/L; To use earlier weight percent concentration be 30% calcium hydroxide is transferred to 9.0 with the pH of L-lactic acid fermentation liquid; Adopt alkaline flocculation agent again and be under 95 ℃ the condition this L-lactic acid fermentation liquid to be carried out flocculation treatment in flocculation temperature; Flocculated 60 minutes, alkaline flocculation agent is a SEPIGEL 305, to remove biomass, protein, thalline, part polysaccharide and other macromolecular substance; Continuation is medium with zeyssatite, through suction filtration and with 50ml deionized water wash filter cake, must 2800ml, L-lactic acid ca concentration is the fermentation clear liquid of 152g/L, and suction filtration can be removed the insolubles of being brought into by calcium hydroxide simultaneously.
C) fermentation clear liquid is carried out acidolysis, filtration treatment, gets the acidolysis cleaner liquid:
The condition of fermentation clear liquid being carried out the acidolysis processing is: the employing weight percent concentration is 98% sulfuric acid, 85 ℃ of temperature, and pressure-controlling is at 0.1bar; Acid hydrolysis solution pH is that acidolysis in 2.5 o'clock finishes, acid hydrolysis solution is carried out suction filtration handles, 2200ml, L-lactic acid concn are the acidolysis cleaner liquid of 135g/L.Present method adopts the low pressure acidolysis, in acidolysis, acid hydrolysis solution is concentrated and remove the volatilizable thing of part low pressure.
D) to the processing of decolouring of acidolysis cleaner liquid, destainer:
To the acidolysis cleaner liquid condition of handling of decolouring be: make the acidolysis cleaner liquid cross the decolouring of carbon post with the flow velocity of 0.5BV/h; The admission space of carbon post is 1000ml; The gac that loads in the carbon post is gac GH-15,2200ml, L-lactic acid concn are the destainer of 132g/L.In the time of decolouring, can remove the organic macromolecules such as protein in the acidolysis cleaner liquid.
E) adopt negatively charged ion absorption exchange resin respectively destainer to be separated, make L-lactic acid and L-Sodium.alpha.-hydroxypropionate:
Let the 1000ml destainer separate with the flow velocity of the 0.5BV/h ion exchange column of flowing through; The admission space of ion exchange column is 1000ml; The negatively charged ion that loads in ion exchange column absorption exchange resin is D201 * 2 vinylbenzene macropore strong alkali resins, and charging is collected waste liquid simultaneously, when reaching the absorption exchange when saturated (when charging is accomplished); As eluent said resin is carried out wash-out with mineral acid; Described mineral acid is the sulfuric acid of 1000ml, 0.5N concentration, and elution flow rate is 0.5BV/h, 1000ml, L-lactic acid concn are the L-lactic acid of 131g/L;
Let the 1000ml destainer separate with the flow velocity of the 0.5BV/h ion exchange column of flowing through; The admission space of ion exchange column is 1000ml; The negatively charged ion that loads in ion exchange column absorption exchange resin is D201 * 4 vinylbenzene macropore strong alkali resins, and charging is collected waste liquid simultaneously, when reaching the absorption exchange when saturated (when charging is accomplished); As eluent said resin is carried out wash-out with mineral alkali; Described mineral alkali is the sodium hydroxide of 1000ml, 0.5N concentration, and elution flow rate is 0.5BV/h, 1000ml, concentration are the L-Sodium.alpha.-hydroxypropionate of 160g/L;
When destainer was flowed through described negatively charged ion absorption exchange resin, the lactate ion that destainer is contained adsorbed exchange with the alkaline reactive group that negatively charged ion adsorbs on the exchange resin.
Embodiment 2:
The preparation method of L-lactic acid and L-Potassium.alpha.-hydroxypropionate comprises following process step successively:
A) prepare the L-lactic acid fermentation liquid through microbial fermentation:
All a) the step with embodiment 1 is identical with parameter to prepare the concrete steps of L-lactic acid fermentation liquid through microbial fermentation in the present embodiment, repeat no more here, and make 2700ml, L-lactic acid ca concentration is the L-lactic acid fermentation liquid of 159g/L.
B) to the L-lactic acid fermentation liquid flocculate, filtration treatment, fermentation clear liquid:
Getting the L-lactic acid ca concentration that a) step makes is the L-lactic acid fermentation liquid 2700ml of 159g/L; To use earlier weight percent concentration be 30% calcium hydroxide is transferred to 10.0 with the pH of L-lactic acid fermentation liquid; Adopt alkaline flocculation agent again and be under 90 ℃ the condition this L-lactic acid fermentation liquid to be carried out flocculation treatment in flocculation temperature; Flocculated 60 minutes, alkaline flocculation agent is a SEPIGEL 305, to remove biomass, protein, thalline, part polysaccharide and other macromolecular substance; Continuation is medium with zeyssatite, through suction filtration and with 50ml deionized water wash filter cake, must 2810ml, L-lactic acid ca concentration is the fermentation clear liquid of 150g/L, and suction filtration can be removed the insolubles of being brought into by calcium hydroxide simultaneously.
C) fermentation clear liquid is carried out acidolysis, filtration treatment, gets the acidolysis cleaner liquid:
The condition of fermentation clear liquid being carried out the acidolysis processing is: the employing weight percent concentration is 98% sulfuric acid, 90 ℃ of temperature, and pressure-controlling is at 0.3bar; Acid hydrolysis solution pH is that acidolysis in 2.0 o'clock finishes, acid hydrolysis solution is carried out suction filtration handles, 2300ml, L-lactic acid concn are the acidolysis cleaner liquid of 128g/L.Present method adopts the low pressure acidolysis, in acidolysis, acid hydrolysis solution is concentrated and remove the volatilizable thing of part low pressure.
D) to the processing of decolouring of acidolysis cleaner liquid, destainer:
To the acidolysis cleaner liquid condition of handling of decolouring be: make the acidolysis cleaner liquid cross the decolouring of carbon post with the flow velocity of 1.8BV/h; The admission space of carbon post is 1000ml; The gac that loads in the carbon post is gac GX830,2300ml, L-lactic acid concn are the destainer of 126g/L.In the time of decolouring, can remove the organic macromolecules such as protein in the acidolysis cleaner liquid.
E) adopt negatively charged ion absorption exchange resin respectively destainer to be separated, make L-lactic acid and L-Potassium.alpha.-hydroxypropionate:
Let the 1000ml destainer separate with the flow velocity of the 1.3BV/h ion exchange column of flowing through; The admission space of ion exchange column is 1000ml; The negatively charged ion that loads in ion exchange column absorption exchange resin is a D202 vinylbenzene macropore strong alkali resin, and charging is collected waste liquid simultaneously, when reaching the absorption exchange when saturated (when charging is accomplished); As eluent said resin is carried out wash-out with mineral acid; Described mineral acid is the hydrochloric acid of 1000ml, 1.0N concentration, and elution flow rate is 1.8BV/h, 1000ml, L-lactic acid concn are the L-lactic acid of 124g/L;
Let the 1000ml destainer separate with the flow velocity of the 1.3BV/h ion exchange column of flowing through; The admission space of ion exchange column is 1000ml; The negatively charged ion that loads in ion exchange column absorption exchange resin is a D202 vinylbenzene macropore strong alkali resin, and charging is collected waste liquid simultaneously, when reaching the absorption exchange when saturated (when charging is accomplished); As eluent said resin is carried out wash-out with inorganic salt; Described mineral alkali is the Repone K of 1000ml, 1.0N concentration, and elution flow rate is 1.8BV/h, 1000ml, concentration are the L-Potassium.alpha.-hydroxypropionate of 178g/L;
When destainer was flowed through described negatively charged ion absorption exchange resin, the lactate ion that destainer is contained adsorbed exchange with the alkaline reactive group that negatively charged ion adsorbs on the exchange resin.
Embodiment 3:
The preparation method of L-lactic acid and L-Potassium.alpha.-hydroxypropionate comprises following process step successively:
A) prepare the L-lactic acid fermentation liquid through microbial fermentation:
The bacillus acidocldarius that the used bacterial classification that ferments is known in the art; Ferment used seed culture medium and preparation thereof, fermention medium prescription and be prepared as the prior art part; Here repeating no more, in the fermention medium is that the glucose of 220g/ L is that carbon source, yeast powder are that nitrogenous source ferments with concentration; Leavening temperature is 50-52 ℃; Flow in real time in the fermenting process and add pH regulator agent adjusting pH value; Making pH is 6.0-6.2; The pH regulator agent concentration that is weight percentage is 25% calcium hydroxide, when glucose has consumed, during fermentation ends, make 2700ml, L-lactic acid ca concentration is the L-lactic acid fermentation liquid of 195g/L.Through the glucose concn in the adjusting fermention medium and the concentration of pH regulator agent, the concentration of coming corresponding adjusting fermented product.
B) the L-lactic acid fermentation liquid is carried out centrifugal treating, gets fermentation clear liquid:
Getting the L-lactic acid ca concentration that a) step makes is the L-lactic acid fermentation liquid 2700ml of 195g/L; Adopt the whizzer of rotating speed 6000rpm that it is carried out centrifugal treating; To remove biomass, protein, thalline, part polysaccharide and other macromolecular substance; And with 50ml deionized water wash filter cake, 2740ml, L-lactic acid ca concentration are the fermentation clear liquid of 190g/L.
C) fermentation clear liquid is carried out acidolysis, filtration treatment, gets the acidolysis cleaner liquid:
The condition of fermentation clear liquid being carried out the acidolysis processing is: the employing weight percent concentration is 98% sulfuric acid, 95 ℃ of temperature, and pressure-controlling is at 0.5bar; Acid hydrolysis solution pH is that acidolysis in 1.5 o'clock finishes, acid hydrolysis solution is carried out suction filtration handles, 2400ml, L-lactic acid concn are the acidolysis cleaner liquid of 148g/L.Present method adopts the low pressure acidolysis, in acidolysis, acid hydrolysis solution is concentrated and remove the volatilizable thing of part low pressure.
D) to the processing of decolouring of acidolysis cleaner liquid, destainer:
To the acidolysis cleaner liquid condition of handling of decolouring be: make the acidolysis cleaner liquid cross the decolouring of carbon post with the flow velocity of 3.0BV/h; The admission space of carbon post is 1000ml; The gac that loads in the carbon post is gac GH-155,2400ml, L-lactic acid concn are the destainer of 147g/L.In the time of decolouring, can remove the organic macromolecules such as protein in the acidolysis cleaner liquid.
E) adopt negatively charged ion absorption exchange resin respectively destainer to be separated, make L-lactic acid and L-Potassium.alpha.-hydroxypropionate:
Let the 1000ml destainer separate with the flow velocity of the 2.0BV/h ion exchange column of flowing through; The admission space of ion exchange column is 1000ml; The negatively charged ion that loads in ion exchange column absorption exchange resin is a D301 vinylbenzene resin and macroporous weak, and charging is collected waste liquid simultaneously, when reaching the absorption exchange when saturated (when charging is accomplished); As eluent said resin is carried out wash-out with mineral acid; Described mineral acid is the nitric acid of 1000ml, 2.0N concentration, and elution flow rate is 3.0BV/h, 1000ml, L-lactic acid concn are the L-lactic acid of 145g/L;
Let the 1000ml destainer separate with the flow velocity of the 2.0BV/h ion exchange column of flowing through; The admission space of ion exchange column is 1000ml; The negatively charged ion that loads in ion exchange column absorption exchange resin is a D301 vinylbenzene resin and macroporous weak, and charging is collected waste liquid simultaneously, when reaching the absorption exchange when saturated (when charging is accomplished); As eluent said resin is carried out wash-out with mineral alkali; Described mineral alkali is the Pottasium Hydroxide of 1000ml, 2.0N concentration, and elution flow rate is 3.0BV/h, 1000ml, concentration are the L-Potassium.alpha.-hydroxypropionate of 208g/L;
When destainer was flowed through described negatively charged ion absorption exchange resin, the lactate ion that destainer is contained adsorbed exchange with the alkaline reactive group that negatively charged ion adsorbs on the exchange resin.
Embodiment 4:
The preparation method of L-lactic acid and L-Sodium.alpha.-hydroxypropionate comprises following process step successively:
A) prepare the L-lactic acid fermentation liquid through microbial fermentation:
All a) the step with embodiment 3 is identical with parameter to prepare the concrete steps of L-lactic acid fermentation liquid through microbial fermentation in the present embodiment, repeat no more here, and make 2700ml, L-lactic acid ca concentration is the L-lactic acid fermentation liquid of 195g/L.
B) the L-lactic acid fermentation liquid is carried out uf processing, gets fermentation clear liquid:
Getting the L-lactic acid ca concentration that a) step makes is the L-lactic acid fermentation liquid 2700ml of 195g/L; Adopt the ultra-filtration membrane of molecular weight cut-off 5000D that it is carried out uf processing; To remove biomass, protein, thalline, part polysaccharide and other macromolecular substance; And with the 400ml deionized water ultrafiltration concentrated phase is dialysed, improving the ultrafiltration yield, 3000ml, L-lactic acid ca concentration are the fermentation clear liquid of 172g/L.
C) fermentation clear liquid is carried out acidolysis, filtration treatment, gets the acidolysis cleaner liquid:
The condition of fermentation clear liquid being carried out the acidolysis processing is: the employing weight percent concentration is 98% sulfuric acid, 90 ℃ of temperature, and pressure-controlling is at 0.2bar; Acid hydrolysis solution pH is that acidolysis in 2.2 o'clock finishes, acid hydrolysis solution is carried out suction filtration handles, 2300ml, L-lactic acid concn are the acidolysis cleaner liquid of 155g/L.Present method adopts the low pressure acidolysis, in acidolysis, acid hydrolysis solution is concentrated and remove the volatilizable thing of part low pressure.
D) to the processing of decolouring of acidolysis cleaner liquid, destainer:
To the acidolysis cleaner liquid condition of handling of decolouring be: make the acidolysis cleaner liquid cross the decolouring of carbon post with the flow velocity of 2.0BV/h; The admission space of carbon post is 1000ml; The gac that loads in the carbon post is gac GX830,2300ml, L-lactic acid concn are the destainer of 153g/L.In the time of decolouring, can remove the organic macromolecules such as protein in the acidolysis cleaner liquid.
E) adopt negatively charged ion absorption exchange resin respectively destainer to be separated, make L-lactic acid and L-Sodium.alpha.-hydroxypropionate:
Let the 1000ml destainer separate with the flow velocity of the 1.5BV/h ion exchange column of flowing through; The admission space of ion exchange column is 1000ml; The negatively charged ion that loads in ion exchange column absorption exchange resin is 700 vinylbenzene resin and macroporous weak, and charging is collected waste liquid simultaneously, when reaching the absorption exchange when saturated (when charging is accomplished); As eluent said resin is carried out wash-out with mineral acid; Described mineral acid is the nitric acid of 1000ml, 1.5N concentration, and elution flow rate is 2.0BV/h, 1000ml, L-lactic acid concn are the L-lactic acid of 151g/L;
Let the 1000ml destainer separate with the flow velocity of the 1.5BV/h ion exchange column of flowing through; The admission space of ion exchange column is 1000ml; The negatively charged ion that loads in ion exchange column absorption exchange resin is 700 vinylbenzene resin and macroporous weak, and charging is collected waste liquid simultaneously, when reaching the absorption exchange when saturated (when charging is accomplished); As eluent said resin is carried out wash-out with inorganic salt; Described inorganic salt are the sodium sulfate of 1000ml, 1.5N concentration, and elution flow rate is 2.0BV/h, 1000ml, concentration are the L-Sodium.alpha.-hydroxypropionate of 190g/L;
When destainer was flowed through described negatively charged ion absorption exchange resin, the lactate ion that destainer is contained adsorbed exchange with the alkaline reactive group that negatively charged ion adsorbs on the exchange resin.
Need to prove: a) the L-lactic acid fermentation liquid in the step can also starch, fructose, beet sugar or its molasses are carbon source, makes through the arbitrary strain fermentation in Lactobacillus amylophilus, lactobacterium casei or the Rhizopus oryzae, and the pH regulator agent also can be lime carbonate; E) mineral alkali described in the step also can be ammoniacal liquor, and described inorganic salt also can be a kind of in SODIUMNITRATE, sodium phosphate, vitriolate of tartar, the potassiumphosphate; In present method, also can prepare L-lactic acid or L-lactic acid salt separately.
Above-described only is four kinds of embodiments of the present invention.Should be pointed out that for the person of ordinary skill of the art under the prerequisite that does not break away from the principle of the invention, can also make some modification and improvement, these also should be regarded as belonging to protection scope of the present invention.
Claims (6)
1.L-the Lactated preparation method of lactic acid and/or L-comprises following process step successively:
A) prepare the L-lactic acid fermentation liquid through microbial fermentation;
B) adopt any method in flocculation and filtration, centrifugal, the ultrafiltration, the L-lactic acid fermentation liquid handled, fermentation clear liquid;
C) fermentation clear liquid is carried out acidolysis, filtration treatment, get the acidolysis cleaner liquid;
D) to the processing of decolouring of acidolysis cleaner liquid, destainer;
E) adopt negatively charged ion absorption exchange resin that destainer is separated, make L-lactic acid and/or L-lactic acid salt.
2. L-lactic acid according to claim 1 and/or the Lactated preparation method of L-is characterized in that:
A) the L-lactic acid fermentation liquid in the step is to be carbon source with starch, glucose, fructose, beet sugar or its molasses; Arbitrary strain fermentation through in Lactobacillus amylophilus, lactobacterium casei, bacillus acidocldarius or the Rhizopus oryzae makes; Flow in real time in the fermenting process and add pH regulator agent adjusting pH value; The weight percent concentration of pH regulator agent is 20-30%, and described pH regulator agent is lime carbonate or calcium hydroxide, makes the L-lactic acid fermentation liquid that L-lactic acid ca concentration is 100-200g/L.
3. L-lactic acid according to claim 1 and/or the Lactated preparation method of L-is characterized in that:
B) first pH with the L-lactic acid fermentation liquid is transferred to 9.0-11.0 in the step, adopts alkaline flocculation agent that this L-lactic acid fermentation liquid is handled again, and flocculation temperature is 90-95 ℃;
Or b) whizzer of employing rotating speed 3000-6000rpm in the step is handled the L-lactic acid fermentation liquid;
Or b) ultra-filtration membrane of employing molecular weight cut-off 1000-20000D in the step is handled the L-lactic acid fermentation liquid.
4. L-lactic acid according to claim 1 and/or the Lactated preparation method of L-is characterized in that:
C) in the step fermentation clear liquid being carried out the condition that acidolysis handles is: temperature 85-95 ℃, pressure-controlling is at 0.01-0.5bar; Acidolysis finished when c) acid hydrolysis solution pH was 1.5-2.5 in the step, and acid hydrolysis solution is carried out filtration treatment, and getting the L-lactic acid concn is the acidolysis cleaner liquid of 100-200g/L.
5. L-lactic acid according to claim 1 and/or the Lactated preparation method of L-is characterized in that:
D) in the step to the acidolysis cleaner liquid condition of handling of decolouring be: make the acidolysis cleaner liquid cross the decolouring of carbon post with the flow velocity of 0.5-3.0BV/h, the gac that loads in the carbon post is any among gac GH-15, the gac GX830.
6. L-lactic acid according to claim 1 and/or the Lactated preparation method of L-is characterized in that:
E) let destainer with the flow velocity of the 0.5-2.0BV/h negatively charged ion absorption exchange resin of flowing through in the step; When reaching absorption exchange when saturated; As eluent said resin is carried out wash-out with mineral acid, get L-lactic acid, as eluent said resin is carried out wash-out with mineral alkali or inorganic salt; Get corresponding L-lactic acid salt; The concentration of eluent is controlled at 0.05-2.0N, flow rate control at 0.5-3.0BV/h, and described negatively charged ion absorption exchange resin is for having the negatively charged ion absorption exchange resin of selecting exchangeability to L-lactic acid, and described mineral acid is any in sulfuric acid, hydrochloric acid, the nitric acid; Described mineral alkali is any in sodium hydroxide, Pottasium Hydroxide, the ammoniacal liquor, and described inorganic salt are any in Repone K, sodium sulfate, SODIUMNITRATE, sodium phosphate, vitriolate of tartar, the potassiumphosphate.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011104215846A CN102517346A (en) | 2011-12-16 | 2011-12-16 | Method for preparing L-lactic acid and/or L-lactate |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011104215846A CN102517346A (en) | 2011-12-16 | 2011-12-16 | Method for preparing L-lactic acid and/or L-lactate |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN102517346A true CN102517346A (en) | 2012-06-27 |
Family
ID=46288412
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2011104215846A Pending CN102517346A (en) | 2011-12-16 | 2011-12-16 | Method for preparing L-lactic acid and/or L-lactate |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102517346A (en) |
Cited By (16)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102976923A (en) * | 2012-12-18 | 2013-03-20 | 青岛科海生物有限公司 | New process for extracting lactic acid from lactic acid fermentation liquid |
| CN102976922A (en) * | 2012-10-30 | 2013-03-20 | 青岛科技大学 | Novel method for recovering calcium lactate by hydrolysis of waste polylactic acid material |
| CN104496796A (en) * | 2015-01-12 | 2015-04-08 | 河南金丹乳酸科技股份有限公司 | Method for rapidly extracting L-lactic acid from ammonium lactate fermented liquid |
| CN105237386A (en) * | 2015-10-27 | 2016-01-13 | 安徽中粮生化格拉特乳酸有限公司 | Environment-friendly lactic acid production technology |
| CN105254486A (en) * | 2015-11-09 | 2016-01-20 | 山东寿光巨能金玉米开发有限公司 | Novel decoloration process for D-lactic acid |
| CN105249399A (en) * | 2015-11-12 | 2016-01-20 | 安徽中粮生化格拉特乳酸有限公司 | Preparation method of solid lactic acid |
| CN105331643A (en) * | 2015-11-03 | 2016-02-17 | 北京联合大学 | Method for preparing L-lactic acid through fermentation of sophora flower bud decoction dregs |
| CN105331026A (en) * | 2015-11-29 | 2016-02-17 | 贵州开磷集团股份有限公司 | Preparation method of CPVC resin filler |
| CN105331010A (en) * | 2015-11-29 | 2016-02-17 | 贵州开磷集团股份有限公司 | Preparation method of PVC resin filler |
| CN105399622A (en) * | 2015-11-20 | 2016-03-16 | 武汉三江航天固德生物科技有限公司 | Method for producing potassium lactate from heavy-component lactic acid |
| CN106754421A (en) * | 2017-01-10 | 2017-05-31 | 台州学院 | A kind of method for controlling to produce L lactic acid bacteria Rhizopus oryzae pellet forms |
| CN111533652A (en) * | 2020-05-25 | 2020-08-14 | 吉林中粮生化有限公司 | Method and system for separating lactate |
| CN112501107A (en) * | 2020-12-02 | 2021-03-16 | 台州学院 | Method for domesticating rhizopus oryzae and method for producing lactic acid |
| CN113121329A (en) * | 2019-12-31 | 2021-07-16 | 中国石油化工股份有限公司 | Method for coupling conversion and extraction of lactic acid from aqueous lactate raw material |
| CN113135954A (en) * | 2021-04-24 | 2021-07-20 | 诸城市浩天药业有限公司 | Process method for preparing calcium phytate and calcium lactate by using corn soaking water |
| US11118006B1 (en) | 2020-06-28 | 2021-09-14 | Nutrition & Health Research Institute, COFCO Corporation | Method for producing polylactic acid |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1009114B (en) * | 1989-03-26 | 1990-08-08 | 河南省郸城县生物化工厂 | Lactic acid prodn. by fermentating and coagulating subsided separation |
| CN100357445C (en) * | 2002-10-22 | 2007-12-26 | 普拉克生化公司 | Separation of biomass from lactic-acid containing fermentation products by means of flocculation |
| CN101555201A (en) * | 2009-05-20 | 2009-10-14 | 安徽丰原格拉特乳酸有限公司 | Acidolysis method of L-calcium lactate fermentation solution |
| CN101130795B (en) * | 2007-07-26 | 2010-05-19 | 武汉三江航天固德生物科技有限公司 | Technique for producing acrylic ester during lactic acid production by zymotechnics |
-
2011
- 2011-12-16 CN CN2011104215846A patent/CN102517346A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1009114B (en) * | 1989-03-26 | 1990-08-08 | 河南省郸城县生物化工厂 | Lactic acid prodn. by fermentating and coagulating subsided separation |
| CN100357445C (en) * | 2002-10-22 | 2007-12-26 | 普拉克生化公司 | Separation of biomass from lactic-acid containing fermentation products by means of flocculation |
| CN101130795B (en) * | 2007-07-26 | 2010-05-19 | 武汉三江航天固德生物科技有限公司 | Technique for producing acrylic ester during lactic acid production by zymotechnics |
| CN101555201A (en) * | 2009-05-20 | 2009-10-14 | 安徽丰原格拉特乳酸有限公司 | Acidolysis method of L-calcium lactate fermentation solution |
Cited By (19)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102976922A (en) * | 2012-10-30 | 2013-03-20 | 青岛科技大学 | Novel method for recovering calcium lactate by hydrolysis of waste polylactic acid material |
| CN102976922B (en) * | 2012-10-30 | 2015-07-15 | 青岛科技大学 | Novel method for recovering calcium lactate by hydrolysis of waste polylactic acid material |
| CN102976923A (en) * | 2012-12-18 | 2013-03-20 | 青岛科海生物有限公司 | New process for extracting lactic acid from lactic acid fermentation liquid |
| CN102976923B (en) * | 2012-12-18 | 2015-06-10 | 青岛科海生物有限公司 | New process for extracting lactic acid from lactic acid fermentation liquid |
| CN104496796A (en) * | 2015-01-12 | 2015-04-08 | 河南金丹乳酸科技股份有限公司 | Method for rapidly extracting L-lactic acid from ammonium lactate fermented liquid |
| CN105237386A (en) * | 2015-10-27 | 2016-01-13 | 安徽中粮生化格拉特乳酸有限公司 | Environment-friendly lactic acid production technology |
| CN105331643A (en) * | 2015-11-03 | 2016-02-17 | 北京联合大学 | Method for preparing L-lactic acid through fermentation of sophora flower bud decoction dregs |
| CN105254486A (en) * | 2015-11-09 | 2016-01-20 | 山东寿光巨能金玉米开发有限公司 | Novel decoloration process for D-lactic acid |
| CN105249399A (en) * | 2015-11-12 | 2016-01-20 | 安徽中粮生化格拉特乳酸有限公司 | Preparation method of solid lactic acid |
| CN105399622A (en) * | 2015-11-20 | 2016-03-16 | 武汉三江航天固德生物科技有限公司 | Method for producing potassium lactate from heavy-component lactic acid |
| CN105331026A (en) * | 2015-11-29 | 2016-02-17 | 贵州开磷集团股份有限公司 | Preparation method of CPVC resin filler |
| CN105331010A (en) * | 2015-11-29 | 2016-02-17 | 贵州开磷集团股份有限公司 | Preparation method of PVC resin filler |
| CN106754421A (en) * | 2017-01-10 | 2017-05-31 | 台州学院 | A kind of method for controlling to produce L lactic acid bacteria Rhizopus oryzae pellet forms |
| CN113121329A (en) * | 2019-12-31 | 2021-07-16 | 中国石油化工股份有限公司 | Method for coupling conversion and extraction of lactic acid from aqueous lactate raw material |
| CN113121329B (en) * | 2019-12-31 | 2022-06-07 | 中国石油化工股份有限公司 | Method for coupling conversion and extraction of lactic acid from aqueous lactate raw material |
| CN111533652A (en) * | 2020-05-25 | 2020-08-14 | 吉林中粮生化有限公司 | Method and system for separating lactate |
| US11118006B1 (en) | 2020-06-28 | 2021-09-14 | Nutrition & Health Research Institute, COFCO Corporation | Method for producing polylactic acid |
| CN112501107A (en) * | 2020-12-02 | 2021-03-16 | 台州学院 | Method for domesticating rhizopus oryzae and method for producing lactic acid |
| CN113135954A (en) * | 2021-04-24 | 2021-07-20 | 诸城市浩天药业有限公司 | Process method for preparing calcium phytate and calcium lactate by using corn soaking water |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102517346A (en) | Method for preparing L-lactic acid and/or L-lactate | |
| CN108285912B (en) | Method for preparing and extracting pharmaceutical grade valine by fermentation | |
| CN113214076B (en) | Method for recovering lactic acid from lactic acid distillation kettle bottom liquid | |
| CN107201387B (en) | Preparation method of iron dextran | |
| CN102976923A (en) | New process for extracting lactic acid from lactic acid fermentation liquid | |
| CN110734884A (en) | Low-salt culture medium and culture method for lactobacillus paracasei | |
| CN103642853A (en) | Novel process for extracting L-malic acid | |
| CN108285913B (en) | Process for preparing and extracting L-glutamine | |
| CN104974032A (en) | Method of separation and extraction of D-lactic acid from sodium D-lactate fermentation liquid | |
| CN102827884B (en) | Method for extracting L-lactic acid produced in corn soaking process | |
| CN104651419A (en) | Method for combined production of mannitol and D-lactic acid by virtue of microorganism anaerobic fermentation | |
| CN104357340A (en) | Method for producing L-malic acid by virtue of biotransformation of fumaric acid | |
| CN107201384A (en) | A kind of method of separation and Extraction D-ALPHA-Hydroxypropionic acid in sodium zymotic fluid from D-ALPHA-Hydroxypropionic acid | |
| CN109136299B (en) | Method for preparing, extracting and purifying threonine | |
| CN103695490B (en) | High-purity arginine production process | |
| CN106244638B (en) | Comprehensive utilization process for producing lactic acid by biomass circulating fermentation | |
| CN113005161A (en) | Preparation method of polysialic acid and polysialic acid product | |
| CN108484692B (en) | Method for efficiently extracting glucosamine from fermentation liquor | |
| CN101597635B (en) | Method for preparing high purity stachyose | |
| CN102040667A (en) | Method for biologically removing protein from sea cucumber polysaccharide | |
| CN105349591B (en) | A kind of natural additive for foodstuff sodium glutamate and its preparation process | |
| CN110724211B (en) | High-value comprehensive utilization method of shrimp and crab shells based on reducing sugar catalytic oxidation and application thereof | |
| CN114230502A (en) | Astaxanthin extraction method | |
| CN104211611A (en) | New fermentation technology of sodium glutamate | |
| CN114230380A (en) | Utilization method of 7-aminocephalosporanic acid production waste |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20120627 |
|
| WD01 | Invention patent application deemed withdrawn after publication |