Extraction of succinic acid with 1-octanol/n-heptane solutions of mixed tertiary amine

The reactive extraction of succinic acid was carried out by mixed tertiary amine which consisted of tripropylamine (TPA) and trioctylamine (TOA) as the extraction agent in 1-octanol/n-heptane diluent. Maximum distribution coefficient was obtained at 8:2 weight ratio of TPA/TOA. At this ratio, its extraction efficiency is above 90% at the 3.9 wt.% of succinic acid in aqueous solution. Furthermore, the prevention of the third phase formation made the phase separation between organic phase and aqueous phase easy.     

Detoxification of hydrolysate by reactive-extraction for generating biofuels

We introduce a reactive extraction to detoxify hydrolysate before fermentation to biofuels. In the selection of diluents, n-octanol showed the highest removal yield of 5-hydroxymethylfurfural (5-HMF) and levulinic acid. The removal yields of inhibitors were normalized to 30-min reactions. In treatments with pure extractant or diluents, only 2 ～ 4.1% of the formic acid was removed. Tri-n-octylamine (extractant) removed levulinic acid and acetic acid more efficiently, and furfural was removed more efficiently than formic acid or 5-HMF. n-Octanol (polar diluent) removed levulinic acid and acetic acid, furfural, and 5-HMF at 21.2, 33.7, and 65.7%, respectively. In contrast, kerosene (inert diluent) only removed the furfural by 27.6%. Based on these results, the optimum reactiveextraction system comprised tri-n-octylamine as the extractant, n-octanol as the polar diluent, and kerosene as the inert diluent. The optimal proportion of complex extractant was 20% trialkylamine, 70% n-octanol, and 10% kerosene. By detoxification, 63.9% of acetic acid and levulinic acid, 24.4% of 5-HMF, 63.9% of formic acid, and 64.0% of furfural could be removed.     

Improved production of (R)-2-octanol via asymmetric reduction of 2-octanone with Oenococcus oeni CECT4730 in a biphasic system

Abstract

Oenococcus oeni CECT4730, which catalyses the asymmetric reduction of 2-octanone to (R)-2-octanol with high enantioselectivity, was further studied to exploit its potential for production of (R)-2-octanol in an aqueous/organic solvent biphasic system. Variables such as the volume ratio of aqueous to organic phase (V_a/V_o), buffer pH, reaction temperature, shaking speed, co-substrates and the ratio of biocatalyst to substrate were examined with respect to the molar conversion, the initial reaction rate and the product enantiomeric excess (e.e.). Under the optimized conditions (V_a/V_o=1:1 (v/v), buffer pH=8.0, reaction temperature=30°C, shaking speed=150 rev/min, ratio of glucose to biomass=5.4:l (w/w), ratio of biocatalyst to substrate=0.51:l (g/mol)), the highest space time yield of (R)-2-octanol, 24 mmol L^?1 per h, and >98% product e.e. were obtained at a substrate concentration close to 1.0 mol L^?1 after 24 h reduction.     

Simultaneous extraction and concentration of penicillin G by hollow fiber renewal liquid membrane

In this article, hollow fiber renewal liquid membrane (HFRLM) technique was used for recovery of penicillin G from aqueous solution. The organic solution of 7 vol % di‐n‐octylamine (DOA) + 30 vol % iso‐octanol + kerosene was used as liquid membrane phase, and Na₂CO₃ aqueous solution was used as stripping phase. Experiments were performed as a function of carrier concentration in the organic phase, organic/aqueous volume ratio, pH, and initial penicillin G concentration in the feed phase, pH in the stripping phase, flow rates, etc. The results showed that the HFRLM process was stable and could carry out simultaneous extraction and concentration of penicillin G from aqueous solutions. As a carrier facilitated transport process, the addition of DOA in organic phase could greatly enhance the mass transfer rate; and there was a favorable organic/aqueous volume ratio of 1:20 to 1:30 for this system. The mass transfer flux and overall mass transfer coefficient increased with decreasing pH in the feed phase and increasing pH in the stripping phase, because of variation of the mass transfer driving force caused by pH gradient and distribution equilibrium. The flow rate of the shell side had significant influence on the mass transfer performance, whereas the effect of flow rate of lumen side on the mass transfer performance was slight because of the mass transfer intensification of renewal effect in the lumen side. The results indicated that the HFRLM process was a promising method for the recovery of penicillin G from aqueous solutions. © 2009 American Institute of Chemical Engineers Biotechnol. Prog., 2009     

New reactive extraction systems for separation of bio-succinic acid

Biotechnologically produced succinic acid has the potential to displace maleic acid and its uses and to become an important feedstock for the chemical industry. In addition to optimized production strains and fermentation processes, an efficient separation of succinic acid from the aqueous fermentation broth is indispensable to compete with the current petrochemical production processes. In this context, high molecular weight amines are known to be effective extractants for organic acids. For this reason, as a first step of isolation and purification, the reactive extraction of succinic acid was studied by mixing aqueous succinic acid solutions with 448 different amine–solvent mixtures as extraction agents (mixer-settler studies). The extraction agents consist either of one amine and one solvent (208 reactive extraction systems) or two amines and two solvents (240 reactive extraction systems). Maximum extraction yields of succinic acid from an aqueous solution with 423 mM succinic acid at pH 2.0 were obtained with more than 95% yield with trihexylamine solved in 1-octanol or with dihexylamine and diisooctylamine solved in 1-octanol and 1-hexanol. Applying these optimized reactive extraction systems with Escherichia coli fermentation broth resulted in extraction yields of 78–85% due to the increased ionic strength of the fermentation supernatant and the co-extraction of other organic acids (e.g., lactic acid and acetic acid), which represent typical fermentation byproducts.     

Extraction and purification of a lectin from small black kidney bean (Phaseolus vulgaris) using a reversed micellar system

Lectin from crude extract of small black kidney bean (Phaseolus vulgaris) was successfully extracted using the reversed micellar extraction (RME). The effects of water content of organic phase (W_o), ionic strength, pH, Aerosol-OT (AOT) concentration and extraction time on the forward extraction and the pH and ionic strength in the backward extraction were studied to optimize the extraction efficiency and purification factor. Forward extraction of lectin was found to be maximum after 15 min of contact using 50 mM AOT in organic phase with W_o 27 and 10 mM citrate-phosphate buffer at pH 5.5 containing 100 mM NaCl in the aqueous phase. Lectin was backward extracted into a fresh aqueous phase using sodium-phosphate buffer (10 mM, pH 7.0) containing 500 mM KCl. The overall yield of the process was 53.28% for protein recovery and 8.2-fold for purification factor. The efficiency of the process was confirmed by gel electrophoresis analysis.     

Stripping of nonionic surfactants from the coacervate phase of cloud point system for lipase separation by Winsor II microemulsion extraction with the direct addition of alcohols

Extractive microbial fermentation of lipase by Serratia marcescens ECU1010 in cloud point system was previously carried out in the cloud point system. The direct addition of different alcohols, including iso-butanol, 2-phenylethanol and 1-octanol, into the coacervate phase of the clear supernatant of the fermentation broth formed microemulsion, where the nonionic surfactants and lipase were unevenly partitioned between the different phases in the microemulsion system. The polarity of alcohols strongly affected the microemulsion type at room temperature condition. The results indicated that the Winsor II microemulsion, formed by the addition of iso-butanol or 2-phenylethanol as the organic solvent, favored the stripping of the nonionic surfactant into the O_m phase, whereas the lipase was left in the excess aqueous phase. However, the Winsor I microemulsion, formed by the addition of 1-octanol as the organic solvent, failed to separate the lipase from the nonionic surfactant in the coacervate phase of cloud point system, because the nonionic surfactant and lipase were partitioned into the W_m phase at the same time. Moreover, in the Winsor II microemulsion extraction with 2-phenylethanol as the organic solvent, in which case the protein–surfactant complexes were absent at the interface between the O_m phase and the excess aqueous phase, the high lipase recovery (above 80%) and good nonionic surfactant removal were achieved. The effect of nonionic surfactants on lipase activity was also presented.     

Liquid membrane extraction of bio-active amphiphilic substances: Recovery of surfactin

The interest of application of liquid membrane (pertraction) processes for recovery of biosurfactants from aqueous media was demonstrated. Transport of pure surfactin in three-liquid-phase system was studied. Surfactin was successfully extracted from slightly acid media (pH 5.65–6.05) applying batch pertraction in a rotating discs contactor and using n-heptane as liquid membrane. The process efficiency was found to be strongly affected by the feed solution acidity (83% at pH_F 6.05 and 97% at pH_F 5.65 after 4 h pertraction).An atypical pH effect was observed when the behaviour of surfactin extraction from aqueous media by non-polar solvents (n-heptane and n-octane) was studied. The obtained high extraction degrees from both acid and basic media and the clearly reduced degree of extraction from neutral media could be attributed to the different conformations of surfactin in these media.     

Bioconversion of p-coumaric acid to p-hydroxystyrene using phenolic acid decarboxylase from B. amyloliquefaciens in biphasic reaction system

Phenolic acid decarboxylase (PAD) catalyzes the non-oxidative decarboxylation of p-coumaric acid (pCA) to p-hydroxystyrene (pHS). PAD from Bacillus amyloliquefaciens (BAPAD), which showed k _cat/K _m value for pCA (9.3?×?10³?mM^?1?s^?1), was found as the most active one using the “Subgrouping Automata” program and by comparing enzyme activity. However, the production of pHS of recombinant Escherichia coli harboring BAPAD showed only a 22.7 % conversion yield due to product inhibition. Based on the partition coefficient of pHS and biocompatibility of the cell, 1-octanol was selected for the biphasic reaction. The conversion yield increased up to 98.0 % and 0.83 g/h/g DCW productivity was achieved at 100 mM pCA using equal volume of 1-octanol as an organic solvent. In the optimized biphasic reactor, using a three volume ratio of 1-octanol to phosphate buffer phase (50 mM, pH 7.0), the recombinant E. coli produced pHS with a 88.7 % conversion yield and 1.34 g/h/g DCW productivity at 300 mM pCA.     

Integrated separation process for isolation and purification of biosuccinic acid

Biotechnologically produced succinic acid has the potential to displace maleic acid and its uses. Therefore, it is of high interest for the chemical, pharmaceutical, and food industry.In addition to optimized production strains and fermentation processes, an efficient separation of succinic acid from the aqueous fermentation broth is indispensable to compete with the current petrochemical production of succinic acid. Isolation and purification of succinic acid from an Escherichia coli fermentation broth were studied with two amine-based reactive extraction systems: (i) trihexylamine in 1-octanol and (ii) diisooctylamine and dihexylamine in a mixture of 1-octanol and 1-hexanol. Back extraction of succinic acid from the organic phase was carried out using an aqueous trimethylamine solution. The trimethylammonium succinate generated after back extraction was split with an evaporation-based crystallization.The focus was on process integration, for example, reuse of the applied amines for extraction and back extraction. It was shown that the maximum trimethylamine concentration for back extraction should not exceed the stoichiometric amount (2 mol trimethylamine/mol the succinic acid in the organic phase) to ensure maximal extraction yields with the reused organic phase in subsequent extractions. Moreover, mixer-settler extraction and back extraction of succinic acid were scaled up from the milliliter- to the liter-scale making use of liquid–liquid centrifuges. The overall yield was 83.5% of the succinic acid from thefermentation supernatant. The final purity of the succinic acid crystals was 99.5%. Organic phase and amines can easily be recycled and reused.     

Predispersed solvent extraction of succinic acid aqueous solution by colloidal liquid aphrons in column

A study of the PDSE (predispersed solvent extraction) for succinic acid by colloidal liquid aphrons was conducted. The organic phase contaning TOA (tri-n-octylamine) and 1-octanol permits a selective extraction of succinic acid from its aqueous solution. There was no difference of the extractability of PDSE and that of conventional mixer-settler type extraction. Taking into account the no mechanical mixing in PDSE, it was concluded that the PDSE process is more adaptive than the conventional mixer-settler type extraction process. From mass transfer analysis at the various concentration of TOA in counter-current continuous operation, the concentration of TOA had no influence on the mass transfer coefficient. The loading values in continuous PDSE were almost same as those in batch operation.     

Reactive extraction of cephalosporin antibiotics in hollow fiber membrane

Non-dispersive reactive extraction of cephalosporin antibiotics has been studied using hollow fiber membrane modules. Extraction as well as stripping has been studied using a pH swing procedure. Cephalosporin was extracted from an aqueous solution of cephalosporin having a pH above the pK_a2 value to an organic phase containing Aliquat-336 as the extractant and n-heptane as the diluent. The solute was stripped from the loaded organic phase to another aqueous phase of pH maintained well below the pK_a2 value of the cephalosporin. The extraction cum stripping relies on pH dependance of the distribution coefficient of cephalosporin in aqueous phase. Reasonably high solute recovery and mass transfer rate have been achieved in the hollow fiber module. Mass transfer performance of a single module has been evaluated and experimentally observed low value of height of transfer unit (HTU) indicates good prospect of hollow fiber membrane for the extraction duty.     

Partition coefficients (n-octanol/water) of N-butyl-p-aminobenzoate and other local anesthetics measured by reversed-phase high-performance liquid chromatography

For the determination of the logarithmic partition coefficients between n-octanol and water (log P_o/w) of local anesthetics, the pH of the aqueous phase needs to be adjusted to high values to ensure that the local anesthetics are in the unionized form. Using the shake-flask or the stir-flask method, this high pH may catalyze hydrolysis, leading to increasing amounts of impurities in time. These impurities exclude non-selective quantification methods like UV spectrometry and require repetitive quantitative analysis of both liquid phases resulting in a tedious and time-consuming method. A rapid reversed-phase HPLC method was developed to measure log P_o/w of the local anesthetics N-butyl-p-aminobenzoate, methyl-p-aminobenzoate, benzocaine, procaine, mepivacaine, prilocaine, lidocaine, bupivacaine, etidocaine, tetracaine and oxubuprocaine.     

Metabolic engineering of Propionibacterium freudenreichii for n-propanol production

Propionibacteria are widely used in industry for manufacturing of Swiss cheese, vitamin B₁₂, and propionic acid. However, little is known about their genetics and only a few reports are available on the metabolic engineering of propionibacteria aiming at enhancing fermentative production of vitamin B₁₂ and propionic acid. n-Propanol is a common solvent, an intermediate in many industrial applications, and a promising biofuel. To date, no wild-type microorganism is known to produce n-propanol in sufficient quantities for industrial application purposes. In this study, a bifunctional aldehyde/alcohol dehydrogenase (adhE) was cloned from Escherichia coli and expressed in Propionibacterium freudenreichii. The mutants expressing the adhE gene converted propionyl- coenzyme A, which is the precursor for propionic acid biosynthesis, to n-propanol. The production of n-propanol was limited by NADH availability, which was improved significantly by using glycerol as the carbon source. Interestingly, the improved propanol production was accompanied by a significant increase in propionic acid productivity, indicating a positive effect of n-propanol biosynthesis on propionic acid fermentative production. To our best knowledge, this is the first report on producing n-propanol by metabolically engineered propionibacteria, which offers a novel route to produce n-propanol from renewable feedstock, and possibly a new way to boost propionic acid fermentation.     

Propionic acid fermentation by Propionibacterium acidipropionici: effect of growth substrate

Summary Batch propionic acid fermentations by Propionibacterium acidipropionici with lactose, glucose, and lactate as the carbon source were studied. In addition to propionic acid, acetic acid, succinic acid and CO₂ were also formed from lactose or glucose. However, succinic acid was not produced in a significant amount when lactate was the growth substrate. Compared to fermentations with lactose or glucose at the same pH, lactate gave a higher propionic acid yield, lower cell yield, and lower specific growth rate. The specific fermentation or propionic acid production rate from lactate was, however, higher than that from lactose. Since about equimolar acid products would be formed from lactate, the reactor pH remained relatively unchanged throughout the fermentation and would be easier to control when lactate was the growth substrate. Therefore, lactate would be a preferred substrate over lactose and glucose for propionic acid production using continuous, immobilized cell bioreactors. Correspondence to: S. T. Yang     

Enantioseparation of N-protected α-amino acid derivatives by liquid-liquid extraction technique employing stereoselective ion-pair formation with a carbamoylated quinine derivative

Two-phase liquid-liquid extraction experiments were undertaken to study the enantioselective transport of the chiral N-protected α-amino acid derivatives from an aqueous buffer solution into an organic phase employing highly lipophilic carbamoylated quinine as chiral selector and phase transfer carrier, respectively. The chiral separation, derived from enantioselective ion-pair formation and differential solubility in the aqueous and organic phases of diastereomeric associates thus formed has been shown to be primarily dependent on the structure of the selectand, the nature of the organic solvent, the molar ratio of a given chiral selector to selectand in the two phases, and the pH of the aqueous phase. Extracted enantiomers were recovered by back-extraction using a relatively polar acidic medium in which the selector is barely insoluble. Thus, the enantiomeric purity of N-(3,5-dinitrobenzoyl)-leucine exceeded 95% enantiomeric excess with 70% overall yield with a single extraction and back-extraction step. Chirality 9:268–273, 1997. © 1997 Wiley-Liss, Inc.     

Integrated L-phenylalanine separation in an E. coli fed-batch process: from laboratory to pilot scale

Pilot-scale reactive-extraction technology for fully integrated L-phenylalanine (L-Phe) separation in Escherichia coli fed-batch fermentations was investigated in order to prevent an inhibition of microbial L-Phe production by-product accumulation. An optimal reactive-extraction system, consisting of an organic kerosene phase with the cation-selective carrier DEHPA (di-2-ethylhexyl phosphonic acid) and an aqueous stripping phase including sulphuric acid, was found particularly efficient. Using this system with two membrane contactors, mass-transfer coefficients of up to 288 x 10(-7) cm s(-1) for the aqueous/organic and 77 x 10(-7) cm s(-1) for the organic/stripping phase were derived from experimental data using a simple modelling approach. Concentration factors higher than 4 were achieved in the stripping phase as compared to the aqueous donor phase. Reactive extraction enabled a 98% cation portion of L-Phe in the stripping phase, leading to final product purity higher than 99% after L-Phe precipitation. A doubling of L-Phe/glucose yield was observed when kerosene/DEHPA was added to the fermentation solution in the bioreactor to experimentally simulate a fully integrated L-Phe separation process.     

Purification of Extracellular Cholesterol Oxidase with High Activity in the Presence of Organic Solvents from Pseudomonas sp. Strain ST-200

Extracellular cholesterol oxidase of Pseudomonas sp. strain ST-200 was purified from the culture supernatant. This oxidase contained bound flavin and was categorized as a 3β-hydroxysteroid oxidase, converting 3β-hydroxyl groups to keto groups. The molecular mass was 60 kDa. The enzyme was stable at pH 4 to 11 and active at pH 5.0 to 8.5, showing optimal activity at pH 7 at 60°C. The Michaelis constant of the ST-200 cholesterol oxidase was lower than those of commercially available oxidases. The cholesterol oxidation rate was enhanced 3- to 3.5-fold in the presence of organic solvents, with log P_ow values (partition coefficients of the organic solvent between n-octanol and water), in the range of 2.1 to 4.2, compared with that in the absence of organic solvents.     

Experimental and Model Studies on Continuous Separation of 2‐Phenylpropionic Acid Enantiomers by Enantioselective Liquid–Liquid Extraction in Centrifugal Contactor Separators

Multistage enantioselective liquid–liquid extraction (ELLE) of 2‐phenylpropionic acid (2‐PPA) enantiomers using hydroxypropyl‐β‐cyclodextrin (HP‐β‐CD) as extractant was studied experimentally in a counter‐current cascade of centrifugal contactor separators (CCSs). Performance of the process was evaluated by purity (enantiomeric excess, ee) and yield (Y). A multistage equilibrium model was established on the basis of single‐stage model for chiral extraction of 2‐PPA enantiomers and the law of mass conservation. A series of experiments on the extract phase/washing phase ratio (W/O ratio), extractant concentration, the pH value of aqueous phase, and the number of stages was conducted to verify the multistage equilibrium model. It was found that model predictions were in good agreement with the experimental results. The model was applied to predict and optimize the symmetrical separation of 2‐PPA enantiomers. The optimal conditions for symmetric separation involves a W/O ratio of 0.6, pH of 2.5, and HP‐β‐CD concentration of 0.1 mol L^?1 at a temperature of 278 K, where ee_eq (equal enantiomeric excess) can reach up to 37% and Y_eq (equal yield) to 69%. By simulation and optimization, the minimum number of stages was evaluated at 98 and 106 for ee_eq > 95% and ee_eq > 97%. Chirality 28:235–244, 2016. © 2016 Wiley Periodicals, Inc. Research highlights are as follows:

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Assessment of toxicity of volatile fatty acids to Photobacterium phosphoreum

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