CN100339357C - Hind extraction process for producing L-phenylalanine using phenyl-pyruvic acid enzyme method - Google Patents
Hind extraction process for producing L-phenylalanine using phenyl-pyruvic acid enzyme method Download PDFInfo
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Abstract
The present invention relates to a hind extraction process for producing L-phenylalanine using a phenyl-pyruvic acid enzyme method, which comprises the following main processing steps: a filtration step of flocculation plate frames of L-phenylalanine conversion liquid is that after filter aids are mixed and blended, the filter aids are driven into the plate frames; a precoating is formed on the filter cloth of the plate frames; flocculating agents and filter aids are filled into the L-phenylalanine conversion liquid produced by the phenyl-pyruvic acid enzyme method; after flocculation, feed liquid is filtered by the plate frames for removing microorganism cells and fragments thereof, and accordingly, filtering liquid is obtained. A simulated moving bed has the following ion-exchange extraction steps: the filtering liquid enters a continuous ion-exchange system for adsorbing; after the adsorption ends, the back washing of impurities is carried out, and then, after eluting agents enter the ion-exchange system for eluting and collecting, eluents are obtained. The product is obtained by the following one-step crystallization steps: after the condensation and the ammonia evaporation of the eluents are carried out, filter cakes are made by making use of activated carbon for the circulation and the filtration of the feed liquid; then, the decolorization, the filtration, the condensation, the crystallization and the drying of the activated carbon are carried out, and accordingly, L-phenylalanine crystal target products are obtained. The present invention can increase the extraction yield of the products and reduce extraction cost.
Description
Technical field
The present invention relates to the back extractive technique that medicine intermediate L-phenylalanine is produced, promptly prepare L-phenylalanine conversion fluid, utilize series of process to realize the high yield of L-phenylalanine, the separation and Extraction of less energy-consumption at enzyme process.
Background technology
The L-phenylalanine is the die aromatischen Aminosaeuren with physiologically active, is that humans and animals can not lean on one of own nature synthetic amino acid, as one of eight essential in body metabolism process seed amino acids; Be mainly used in: use safely in any food-drink (1); Be used for food, can make an addition in the bakery product, strengthen the trophism of phenylalanine; Also with carbohydrate generation amino-carboxylation reaction improving food using, and additional needed by human body functional foodstuff amino acid balance; It is the main raw material of synthetic dipeptide sweetener aspartame (Aspartame); (2) be used for medicine, it is the intermediate of amino acids cancer therapy drugs such as phenylpropyl alcohol ammonia benzyl, formic acid Sarkolizin, also being to produce suprarenin, thyroxine and melanic raw material, is the important composition of preparation amino acid transfusion and comprehensive amino acid preparation, is used for synthetic antiviral, vitamin B6 etc.In recent years, because aspartame has become world market popular sweetener product the most, obtained using widely, so become the maximum impetus that promotes L-phenylalanine rush of demand at food, beverage industry.
The industrialized process for preparing of L-phenylalanine mainly contains fermentation method and enzyme process.Production by Enzymes L-phenylalanine has production concentration height, few, the strong advantage of throughput of purification step, is the main production route of current L-phenylalanine.Production by Enzymes L-phenylalanine has two kinds of cinnamic acid enzymatic and phenyl-pyruvic acid enzyme process again, the phenyl-pyruvic acid enzyme process has greater advantage at aspects such as production technique, production costs than cinnamic acid enzymatic, so thought most economical, the most promising L-phenylalanine production method by current domestic and international research department.
In phenyl-pyruvic acid enzymatic conversion method liquid, except reaction substrate phenyl-pyruvic acid, L-aspartic acid and main components such as reaction product L-phenylalanine and pyruvic acid, also have microorganism cells and multiple compositions such as fragment, foreign protein, inorganic salt and pigment thereof.Therefore select the extraction process of L-phenylalanine of economical rationality very important to the market competitiveness that improves the L-phenylalanine.The extracting method of existing report mainly contains:
1, batch ion exchange extraction method: under pH＜3 and pH＞10 conditions, the L-phenylalanine in the ADSORPTION IN A FIXED BED conversion fluid of utilization filling Zeo-karb (3～5g/L), through alkaline and acidic solution wash-out, the concentrated L-phenylalanine that obtains;
2, calcium salt precipitation method: utilize calcium ion and phenylalanine to form infusible precipitate, form precipitation between pH8.5～11, the phenylalanine calcium salt obtains phenylalanine through hydrochloric acid neutralization, crystallization;
3, the zinc salt precipitator method: with sodium hydrate regulator solution pH7～9, in solution, add the zinc sulfate solid again and obtain phenylalanine zinc salt precipitation, obtain the L-phenylalanine through acid neutralization, crystallization;
4, membrane technique extraction method: utilize microorganism cells and fragment thereof in inorganic ceramic film or the organic membrane filter removal conversion fluid, remove albumen with ultra-filtration membrane then,, after crystallization, obtain the L-phenylalanine through nanofiltration membrane decolouring, desalination and concentrated.
5, continuous ionic exchange extraction process: at first L-phenylalanine conversion fluid is utilized centrifuging to remove microorganism cells and fragment thereof, entering the continuous ionic exchange system then adsorbs, after being adsorbed to finite concentration, carry out wash-out with eluent, collect elutriant, after concentrated, crystallization and drying, obtain the L-phenylalanine again.
From the effect and the economic analysis of operating procedure, extraction, the equal defectiveness of above-mentioned method.In the extracting method of having reported, conversion fluid is removed microorganism cells and fragment thereof, most employing centrifuging operations, and this centrifugal effect is poor, and filter loss is bigger, needs cleaning filter residue in time; In the batch ion exchange process, concentration in the upper prop liquid is on the low side (3～5g/L), the utilization ratio of upper prop resin low (being generally 60～70%), eluent consumption is big, and the activation of resin, regeneration and cleaning need consume a large amount of soda acids, cause whole extraction cost higher; Produce a large amount of salt and waste water in the metal salt precipitate, and the purity of its extract yield and product is all lower; Higher in the membrane separation technique owing to the film device price, and the maintenance cost of film is higher, and the extraction cost of product is too high; In the continuous ionic exchange extraction process, the quality of elutriant (such as transmittance) is poor, and the concentration ratio of elutriant is lower; The said extracted method, generally need first crystallization to obtain crude product after, obtain elaboration by refining again, waste energy consumption like this, in the said extracted method, contain a large amount of impurity in the mother liquor, recovery utilization rate is low.Therefore, develop high yield, L-phenylalanine extracting method promotes the industrialization of L-phenylalanine to seem most important cheaply.
Summary of the invention
Summary of the invention the objective of the invention is to overcome above-mentioned deficiency, provides a kind of and can improve the extract yield of product and reduce extraction cost, satisfies the back extraction process of the needs phenyl-pyruvic acid Production by Enzymes L-phenylalanine of industrialized production.
The object of the present invention is achieved like this: a kind of back extraction process of phenyl-pyruvic acid Production by Enzymes L-phenylalanine, it is characterized in that its processing step comprises: the conversion fluid flocculation Plate Filtration of L-phenylalanine, simulation moving-bed ion exchange extraction and disposable crystallization go out product, and each processing step specifically comprises:
The conversion fluid flocculation Plate Filtration of step 1, L-phenylalanine
1. make precoated layer: will squeeze in the sheet frame behind the flocculating aids stirring and evenly mixing, on the sheet frame filter cloth, form precoated layer, precoated layer thickness 0.5～8mm,
2. the conversion fluid of L-phenylalanine flocculation: in the conversion fluid of phenyl-pyruvic acid Production by Enzymes L-phenylalanine, add flocculation agent and flocculating aids, stir, leave standstill,
3. the feed liquid after will flocculating is removed microorganism cells and fragment thereof by forming the precoated layer Plate Filtration, gets filtered liquid;
Step 2, simulation moving-bed ion exchange extraction
1. the filtered liquid with step 1 is the upper prop liquid of ion-exchange; Upper prop liquid enters the mouth with 1～5m from sample introduction liquid
3/ h speed enters in the continuous ionic exchange system adsorbs, and in the adsorption process, absorption pH value is controlled at 1～3, and adsorption time is 1～5h,
2. after absorption finished, it was assorted to carry out backwash with pure water from the assorted inlet of ion exchange system backwash,
3. eluent is heated to 20～60 ℃, from the eluent ingress, with 2～5m
3/ h enters ion exchange system and carries out wash-out, is to begin to collect elutriant at 2～4 o'clock at wash-out pH, is to stop to collect in 10～11 o'clock until pH, obtains elutriant;
Step 3, disposable crystallization go out product
The elutriant that step 2 is obtained, after concentrating ammonia still process, utilize gac to make filter cake earlier, carry out the feed liquid circulating filtration, carry out activated carbon decolorizing again, bleaching temperature is 30～80 ℃, the pH value is 2.5～6, bleaching time 20～80min filters, concentrates, crystallization, drying, obtains L-phenylalanine crystal target product.
Its transmittance was lower than 10% after above-mentioned elutriant concentrated ammonia still process, feed liquid by gac filter cake circulating filtration after the feed liquid transmittance reach 25～40%, during activated carbon decolorizing, activated carbon dosage only needs 0.05～0.2%.
The back extraction process of phenyl-pyruvic acid Production by Enzymes L-phenylalanine of the present invention, described processing step also includes the recovery of step 4, mother liquor: the mother liquor that obtains after step 3 is extracted goes out target product by the described flocculation Plate Filtration of step 1, the described simulation moving-bed ion exchange extraction of step 2 and the described disposable crystallization of step 3 again.
The mother liquor that obtains after using the step 3 method to extract, impurity such as inorganic salt are fewer comparatively speaking, but as with its product that directly decolours and concentrate out, the purity of its product, transmittance and limit index etc. are all defective, after adopting the flocculation Plate Filtration among the present invention, carry out ion exchange extraction, again through the product that concentrates, crystallization obtains, quality is higher, the conformance with standard requirement.
The back extraction process of phenyl-pyruvic acid Production by Enzymes L-phenylalanine of the present invention, the described flocculation agent of step 1 adopt a kind of in polyacrylamide, Tai-Ace S 150 or the polymerize aluminum chloride or several, and its dosage is 0.8%～1.5% volume percent of L-phenylalanine.
The back extraction process of phenyl-pyruvic acid Production by Enzymes L-phenylalanine of the present invention, the described flocculating aids of step 1 adopt a kind of in pearlife, silicon bath soil or the perlite or several, and its dosage is 3%～5% volume percent of flocculation agent.
Above-mentioned steps two described eluents of the present invention are alkaline aqueous solution, as liquid caustic soda, ammoniacal liquor etc., can reclaim and re-use.
During the described whole ion exchange process of above-mentioned steps of the present invention two, the chuck of ion exchange column must be incubated at 40～90 ℃.
The present invention has following advantage:
1, the conversion fluid flocculation Plate Filtration of the L-phenylalanine of the present invention's employing, suitable flocculation agent, flocculating aids have been selected, its filtration velocity is than very fast, filtering effect is relatively good, the turbidity of filtered liquid is below 100NTU, and transmittance is greater than 50%, and filtering loss is smaller, generally below 1%, such filter effect can guarantee that disposable crystalline product conforms to quality requirements.
2, the ion exchange extraction technology of the present invention's employing is being carried out effective control to absorption terminal point, wash-out terminal point, and the concentration of the elutriant that obtains is higher, reduces the steam of the concentrated consumption of next procedure, the consumption of save energy greatly;
3, the ion exchange extraction technology of the present invention's employing, it is assorted to carry out backwash after the absorption, and the quality of elutriant is significantly improved then, and its transmittance can be greater than 45%;
4, the ion exchange extraction technology that adopts of the present invention is incubated the chuck of eluent and ion exchange column, prevents that the L-phenylalanine from separating out, and makes resin harden and causes the decline of adsorptive power.
5, eluent is recycled, and can reduce cost.
6, disposable crystallization is qualified product, has reduced the energy of the required consumption of secondary crystal.
When 7, product decolours, utilize the waste active carbon after decolouring to make the gac filter cake, carry out circulating filtration earlier, and then carry out the decolorization experiment of gac, so not only saved the consumption of gac, and improved decolorizing effect.
8, the reasonable use of mother liquor does not influence the quality of product, makes the yield of product improve.
Description of drawings
Fig. 1 is an extraction process process operation synoptic diagram of the present invention.
Embodiment
Embodiment 1:
Referring to Fig. 1, Fig. 1 is an extraction process process operation synoptic diagram of the present invention.Its processing step comprises: the recovery that the conversion fluid flocculation Plate Filtration of L-phenylalanine, simulation moving-bed ion exchange extraction, disposable crystallization go out product and mother liquor, and each processing step specifically comprises:
The conversion fluid flocculation Plate Filtration of step 1, L-phenylalanine
1. prepare flocculating aids and flocculation agent:
Under normal temperature condition, prepare flocculating aids, in the reactor of 5T, add 2.5T water, drop into a kind of in flocculating aids pearlife, silicon bath soil or the perlite of 120kg or several, standby.
The preparation flocculation agent: in the reactor of 30T, add 15T water, elevated temperature to 65 ℃ drops into a kind of in flocculation agent polyacrylamide, Tai-Ace S 150 or the polymerize aluminum chloride of 280kg or several, be stirred to dissolving after, be cooled to 25 ℃; Standby.
2. make precoated layer: form precoated layer, precoated layer thickness 3mm with squeezing into sheet frame behind the flocculating aids stirring and evenly mixing; Standby.To squeeze in the sheet frame behind the flocculating aids stirring and evenly mixing, on the sheet frame filter cloth, form precoated layer, precoated layer thickness 0.5～8mm.
3. the conversion fluid of L-phenylalanine flocculation: in the phenyl-pyruvic acid Production by Enzymes L-of 20T phenylalanine conversion fluid, add above-mentioned flocculation agent 2000L for preparing and the flocculating aids of 60L, behind the stirring 15min, leave standstill 45min,
4. the feed liquid after will flocculating is removed microorganism cells and fragment thereof by forming the precoated layer Plate Filtration, gets filtered liquid, filters the turbidity 80NTU of back solution, transmittance 56%, yield 99.0%.
Step 2, simulation moving-bed ion exchange extraction
Get the filtered liquid 10m that obtains in the step 1
3, the concentration 15g/L of L-phenylalanine is with 3m
3The input speed of/h enters ion exchange system, and absorption pH value is controlled at 1.8, behind the about 2.5h of adsorption time, is 5m with flow velocity
3The pure water of/h carries out the assorted 25min of backwash, and with the eluent liquid caustic soda of 0.5mol/L, temperature is heated to 40 ℃, with 2.5m again
3The L-phenylalanine that the flow velocity of/h will be adsorbed on the resin elutes, and chuck need be incubated 80 ℃, begins to collect the height stream of elutriant when pH is 2.5, stops in 10.8 o'clock until being collected into pH.Its elutriant transmittance is 54.0%, and yield is 98.9%.
Step 3, disposable crystallization go out product
Get the elutriant 9m that obtains in the above-mentioned steps two
3, its concentration is 32.5g/L, concentrates ammonia still process 35min, with feed liquid cycle through utilize waste active carbon to make cake filtration 45min after, feed liquid is squeezed into bleacher, add the gac of 10kg, bleaching temperature is 68 ℃, the pH value is 5, and bleaching time 30min filters, concentrates, crystallization, drying, obtain L-phenylalanine crystal 2 90.2kg, its yield is 99.2%, and purity is 99.6%, transmittance 99.5%, specific rotatory power are-34.0 °, and limit index is all qualified.
The recovery of step 4, mother liquor
Get the mother liquor that obtains after step 3 is extracted, after thin up to concentration is 15g/L,, one require to prepare the flocculating aids pearlife set by step, flocculation agent polyacrylamide and make the sheet frame precoated layer, precoated layer thickness 3mm to the Plate Filtration that flocculates; After in mother liquor, adding flocculation agent polyacrylamide, the stirring of flocculating aids pearlife, remove impurity by forming the precoated layer Plate Filtration, to filter good solution process again from friendship, condensing crystal etc., the purity of product is 99.0%, transmittance 99.0%, specific rotatory power are-33.6 °, and limit index is all qualified.
Embodiment 2:
In the phenyl-pyruvic acid Production by Enzymes L-of 20T phenylalanine conversion fluid, add flocculation agent Tai-Ace S 150 1800L, flocculating aids silicon bath soil 90L behind the stirring 25min, leaves standstill 30min; Remove microorganism cells and fragment thereof by form layers Plate Filtration, obtain filtered liquid, filter the turbidity 85NTU of back solution, transmittance 54%, yield 99.2%.All the other are with embodiment 1.
Embodiment 3:
Get filtered liquid 10m among the embodiment 2
3, the concentration 15g/L of L-phenylalanine is with 2m
3The input speed of/h enters from the friendship system, and absorption pH value is controlled at 1.6, behind the about 3h of adsorption time, is 4m with flow velocity
3The pure water of/h carries out the assorted 20min of backwash, and with the eluent ammoniacal liquor of 0.4mol/L, temperature is heated to 35 ℃, with 2m again
3The L-phenylalanine that the flow velocity of/h will be adsorbed on the resin elutes, and chuck need be incubated 75 ℃, begins to collect the height stream of elutriant when pH is 2, stops in 10.7 o'clock until being collected into pH.Its elutriant transmittance is 52.0%, and yield is 99.2%.All the other are with embodiment 1.
Embodiment 4:
Get the filtered liquid 10m that obtains among the embodiment 1
3, the concentration 15g/L of L-phenylalanine is with 4m
3The input speed of/h enters from the friendship system, and absorption pH value is controlled at 2.0, behind the about 2h of adsorption time, is 6m with flow velocity
3The pure water of/h carries out the assorted 15min of backwash, and with the eluent of 0.3mol/L, temperature is heated to 45 ℃, with 3m again
3The L-phenylalanine that the flow velocity of/h will be adsorbed on the resin elutes, and chuck need be incubated 80 ℃, begins to collect the height stream of elutriant when pH is 3, stops in 10.5 o'clock until being collected into pH.Its elutriant transmittance is 48.0%, and yield is 99.0%.
Embodiment 5:
Get the elutriant 9m that obtains in embodiment 1 step 2
3, its concentration is 34.0g/L, concentrates ammonia still process 40min, with feed liquid cycle through utilize waste active carbon to make cake filtration 50min after, feed liquid is squeezed into bleacher, add the gac of 8.5kg, bleaching temperature is 70 ℃, the pH value is 4.8, and bleaching time 35min filters, concentrates, crystallization, drying, obtain L-phenylalanine crystal 3 02.5kg, its yield is 98.9%, and purity is 99.7%, transmittance 99.2%, specific rotatory power are-33.9 °, and limit index is all qualified.All the other are with embodiment 1.
Embodiment 6:
Get the elutriant 9m that obtains in the foregoing description 4
3, its concentration is 31.8g/L, concentrates ammonia still process 30min, with feed liquid cycle through utilize waste active carbon to make cake filtration 40min after, feed liquid is squeezed into bleacher, add the gac of 9kg, bleaching temperature is 65 ℃, the pH value is 4.2, and bleaching time 40min filters, concentrates, crystallization, drying, obtain L-phenylalanine crystal 2 82.4kg, its yield is 98.7%, and purity is 99.4%, transmittance 99.3%, specific rotatory power are-34.1 °, and limit index is all qualified.All the other are with embodiment 1.
Embodiment 7:
Get the mother liquor that obtains in the foregoing description 5,6, after thin up to concentration is 12g/L,, prepare flocculating aids, flocculation agent II and make the sheet frame precoated layer, precoated layer thickness 2mm by embodiment 1 requirement to the Plate Filtration that flocculates; Mother liquor is added after flocculation agent II, flocculating aids 3% stir, remove impurity by forming the precoated layer Plate Filtration, will filter good solution process again from friendship, condensing crystal etc., the purity of product is 99.1%, transmittance 98.9%, specific rotatory power are-33.7 °, and limit index is all qualified.
Claims (7)
1, a kind of back extraction process of phenyl-pyruvic acid Production by Enzymes L-phenylalanine, it is characterized in that its processing step comprises: the conversion fluid flocculation Plate Filtration of L-phenylalanine, simulation moving-bed ion exchange extraction and disposable crystallization go out product, and each processing step specifically comprises:
The conversion fluid flocculation Plate Filtration of step 1, L-phenylalanine
1. make precoated layer: will squeeze in the sheet frame behind the flocculating aids stirring and evenly mixing, on the sheet frame filter cloth, form precoated layer, precoated layer thickness 0.5～8mm,
2. the conversion fluid of L-phenylalanine flocculation: in the conversion fluid of phenyl-pyruvic acid Production by Enzymes L-phenylalanine, add flocculation agent and flocculating aids, stir, leave standstill,
3. the feed liquid after will flocculating is removed microorganism cells and fragment thereof by forming the precoated layer Plate Filtration, gets filtered liquid;
Step 2, simulation moving-bed ion exchange extraction
1. the filtered liquid with step 1 is the upper prop liquid of ion-exchange; Upper prop liquid enters the mouth with 1～5m from sample introduction liquid
3/ h speed enters in the continuous ionic exchange system adsorbs, and in the adsorption process, absorption pH value is controlled at 1～3, and adsorption time is 1～5h,
2. after absorption finished, it was assorted to carry out backwash with pure water from the assorted inlet of ion exchange system backwash,
3. eluent is heated to 20～60 ℃, from the eluent ingress, with 2～5m
3/ h enters ion exchange system and carries out wash-out, is to begin to collect elutriant at 2～4 o'clock at wash-out pH, is to stop to collect in 10～11 o'clock until pH, obtains elutriant,
Step 3, disposable crystallization go out product
The elutriant that step 2 is obtained, after concentrating ammonia still process, utilize gac to make filter cake earlier, carry out the feed liquid circulating filtration, carry out activated carbon decolorizing again, bleaching temperature is 30～80 ℃, the pH value is 2.5～6, bleaching time 20～80min filters, concentrates, crystallization, drying, obtains L-phenylalanine crystal target product.
2, the back extraction process of a kind of phenyl-pyruvic acid Production by Enzymes L-phenylalanine according to claim 1, it is characterized in that processing step also includes the recovery of step 4, mother liquor: the mother liquor that obtains after step 3 is extracted goes out target product by the described flocculation Plate Filtration of step 1, the described simulation moving-bed ion exchange extraction of step 2 and the described disposable crystallization of step 3 again.
3, the back extraction process of a kind of phenyl-pyruvic acid Production by Enzymes L-phenylalanine according to claim 1 and 2, it is characterized in that the described flocculation agent of step 1 adopts a kind of in polyacrylamide, Tai-Ace S 150 or the polymerize aluminum chloride or several, its dosage is 0.8%～1.5% volume percent of L-phenylalanine.
4, the back extraction process of a kind of phenyl-pyruvic acid Production by Enzymes L-phenylalanine according to claim 1 and 2, it is characterized in that the described flocculating aids of step 1 adopts a kind of in pearlife, silicon bath soil or the perlite or several, its dosage is 3%～5% volume percent of flocculation agent.
5, the back extraction process of a kind of phenyl-pyruvic acid Production by Enzymes L-phenylalanine according to claim 1 and 2 is characterized in that the described eluent of step 2 is an alkaline aqueous solution.
6, the back extraction process of a kind of phenyl-pyruvic acid Production by Enzymes L-phenylalanine according to claim 5 is characterized in that described alkaline aqueous solution is an ammoniacal liquor.
7, the back extraction process of a kind of phenyl-pyruvic acid Production by Enzymes L-phenylalanine according to claim 1 and 2, when it is characterized in that the described whole ion exchange process of step 2, the chuck insulation of ion exchange column is at 40～90 ℃.
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS60188353A (en) * | 1984-03-08 | 1985-09-25 | Nippon Kayaku Co Ltd | Decoloring purification of amino acid |
| TW285665B (en) * | 1993-06-18 | 1996-09-11 | Dev Center Biotechnology | Process for purifying L-phenylalnine |
| CN1616415A (en) * | 2004-09-15 | 2005-05-18 | 南京工业大学 | Continuous Ion Exchange Extraction Process of L-Phenylalanine |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS60188353A (en) * | 1984-03-08 | 1985-09-25 | Nippon Kayaku Co Ltd | Decoloring purification of amino acid |
| TW285665B (en) * | 1993-06-18 | 1996-09-11 | Dev Center Biotechnology | Process for purifying L-phenylalnine |
| CN1616415A (en) * | 2004-09-15 | 2005-05-18 | 南京工业大学 | Continuous Ion Exchange Extraction Process of L-Phenylalanine |
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