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Feasibility of Propionic Acid Production by Extractive Fermentation Zhong Gu, David A

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Feasibility of Propionic Acid Production by Extractive Fermentation Zhong Gu, David A Feasibility of propionic acid production by extractive fermentation Zhong Gu, David A. Rickert, Bonita A. Glatz, Charles E. Glatz To cite this version: Zhong Gu, David A. Rickert, Bonita A. Glatz, Charles E. Glatz. Feasibility of propionic acid produc- tion by extractive fermentation. Le Lait, INRA Editions, 1999, 79 (1), pp.137-148. hal-00929629 HAL Id: hal-00929629 https://hal.archives-ouvertes.fr/hal-00929629 Submitted on 1 Jan 1999 HAL is a multi-disciplinary open access L’archive ouverte pluridisciplinaire HAL, est archive for the deposit and dissemination of sci- destinée au dépôt et à la diffusion de documents entific research documents, whether they are pub- scientifiques de niveau recherche, publiés ou non, lished or not. The documents may come from émanant des établissements d’enseignement et de teaching and research institutions in France or recherche français ou étrangers, des laboratoires abroad, or from public or private research centers. publics ou privés. Lait (1999) 79, 137-148 137 © Inra/Elsevier, Paris Original article Feasibility of propionic acid production by extractive fermentation Zhong Gua, David A. Rickert", Bonita A. Glatz", Charles E. Glatza* a Department of Chemical Engineering, Iowa State University, Ames. lA, USA b Department of Food Science and Human Nutrition, Iowa State University, Ames, lA, USA Abstract - Production of propionic acid by fermentation is hindered by low productivity and prod- uct inhibition. Cell immobilization to increase productivity and extractive fermentation to reduce product inhibition were investigated. Propionic acid concentration in the extractive fermentation was maintained at 13 g·L-1 by concurrent extraction with a Iiquid extractant consisting of 40 % (v/v) Alamine" 304-1 (trilaurylamine) in Witcohol" 85 NF (oleyl alcohol). A final concentration of71 g-L-1 propionic acid was obtained in non extractive mode. Yields of propionic and acetic acids were dou- bled and higher overall productivities were obtained in the extractive fermentation. The extractant also exhibited selectivity for propionic acid over acetic acid, thus partially purifying the former. In both fermentation modes, productivity was enhanced by cell immobilization in calcium alginate beads. An economie analysis of a modified version of the fermentation based on several favorable assump- tions showed that the extractive fermentation can, at best, approach economie feasibility at an annual production of 4.7 x 107 kg. For the assumed conditions, the production cost of the propionic acid was US$ 1.16·kg-'; this cost was reduced to US$ 0.94·kg-' when the value of the acetic acid byproduct was included. © Inra/Elsevier, Paris. extractive fermentation / propionic acid / propionibacteria / economie Résumé - Étude de faisabilité de la production d'acide propionique par fermentation extrac- tive. La production d'acide propionique par fermentation rencontre deux obstacles: la faible pro- ductivité et l'inhibition par le produit. L'immobilisation de cellule pour augmenter la productivité et la fermentation extractive pour réduire l'inhibition par le produit ont été étudiées. La concentration en acide propionique en fermentation extractive était maintenue à 13 g-L'" par extraction en co-cou- rant avec un liquide d'extraction composé à 40 % (v/v) d'Alumine" 304-1 (trilaurylamine) dans du Witcohol" 85NF (oleyl alcool). Une concentration finale de 71 g-L:' en acide propionique était obte- nue en mode non-extractif. Les rendements en acides propionique et acétique étaient doublés et une productivité globale supérieure était obtenue en fermentation extractive. Le liquide d'extraction montrait de plus une sélectivité en faveur de l'acide propionique par rapport à l'acide acétique, conduisant à une purification partielle. Dans les deux modes de fermentation, la productivité était aug- Oral communication at the 2nd Symposium on Propionibacteria, Cork, lreland, June 25-27, 1998. * Correspondence and reprints. [email protected] 138 Z. Gu et al. mentée par l'immobilisation des cellules dans des billes d'alginate de calcium. Une analyse écono- mique de la version modifiée de la fermentation basée sur ces hypothèses les plus favorables a mon- tré que la fermentation extractive peut, au mieux, approcher la faisabilité économique pour une pro- duction annuelle de 4,7 x 107 kg. Dans les conditions envisagées, le coût de production de l'acide propionique était de 1,16 $·kg-1; ce coût était réduit à 0,94 $·kg-1 lorsque l'on incluait la valeur du coproduit acide acétique. © InraJElsevier, Paris. fermentation extractive / acide propionique / bactérie propionique / économie 1. INTRODUCTION boxylic acids including propionic acid [l, 7,22-24]. Among separation methods, liq- Propionic acid is a commodity chemical uid-liquid extraction is the most widely stud- with uses in animal feed, grain preserva- ied. Several extractive fermentation pro- tion, antifungal agents (calcium and sodium cesses for propionic acid were developed salts), plasticizers (cellulose acetate propi- using several complex solvent systems [13, onate) and herbicides. The synthesis of pro- 16,21]. Solichien et al. [21] used a hollow- pionic acid has so far been dominated by fiber module for membrane extraction petrochemical routes, including the oxida- of propionic acid with 200 g-L-1 TOPO tion of propane, propionaldehyde, and (tri-n-octyl phosphine oxide, extractant) in propanol. This makes the product very vul- kerosene (diluent). This solvent system was nerable to the sudden priee fluctuations of nontoxic to the propionibacteria. However, propane and natural gas. On the other hand, the integrity of the hollow-fiber module was synthe sis by fermentation is able to utilize hard to maintain because of solvent crys- inexpensive and renewable biomass as sub- tallization at room temperature. Propionic strate [3, 9,10,12,14,17,25]. acid was also extracted with 100 g-L:" Commercialization of a propionic acid TOPO in n-decane (as solvent) in a flat fermentation process must overcome three sheet, supported liquid membrane (SLM) barriers. First, the fermentation is lengthy. apparatus by Ozadali et al. [16]. The stabil- A typical batch fermentation takes about ity of the SLM was limited by leaching of 3 d to reach 20 g·L-1 propionic acid, with the n-decane. Lewis and Yang [13] used a yield (the mass of the acid formed per unit 40 % (w/w) Alamine'" 336 in 2-octanol to mass of the substrate consumed) usually extract propionic acid via two modes of less than 60 % [8]. Second, the fermenta- extraction. With in situ extraction, direct tion is end-product-inhibited [26], which contact of the microorganism and the sol- limits the final propionic acid concentra- vent caused acid productivity to decrease; tion. Third, downstream separation and con- the fermentation was not inhibited by ex centration of the acid are expensive because situ extraction. of its low concentration (usually less than The economie feasibility of the propi- 1 60 g.L- propionic acid) and the presence onic acid fermentation process has been of acetic acid as a byproduct. The low addressed [2,13,15]. Lewis and Yang [13] volatility of propionic acid relative to water reported that 16400 kg of calcium propionate makes recovery by direct distillation prob- could be produced daily from 450 000 kg lematic. of whey for about US$ 0.34·kg-1 of prod- Integration of separation and fermenta- uet. However, they gave no details on down- tion as a means of overcoming sorne of these stream processing eosts. Clausen and Gaddy barriers has been considered for several car- [2] presented preliminary designs for a plant Propionie acid fermentation 139 with an annual production of3.2 x 107 kg at fermentations was 40 %. The fermenter and costs of US$ 0.46·kg-1 andUS$ 0.54·kg-1 accessory controls were previously described [20]. A constant pH at 6 or 7 was maintained via for acetic and propionic acids, respectively the automatie addition of6 mol-L:' NaOH. The (1981 values). Nishikawa et al. [15] stud- temperature was 32 "C and the culture was agi- ied co-production of other valuable prod- tated at ISO rpm. Glucose was monitoréd with a YSI enzymatic glucose/lactate analyzer (Model ucts such as vitamin B12 with propionic acid to improve the economie viability of the fer- 2700, Yellow Springs, Inc., Yellow Springs, OH) 1 mentation process. and was maintained between 35 and 75 g-L- by feeding appropriate amounts of a 500 g-L-1 glu- Previously we found that 40 % (v/v) cose solution. An aliquot of 10 x glucose-free Alamine" 304-1 (trilaurylamine) in FB was also fed every 24 h to replenish other Witcohol'" 85 NF (oleyl alcohol) was non- nutrients. toxic, provided good partitioning of propi- For extractive fermentation in 300 mL FB, onic acid into the solvent, and was compat- the solvent reservoir contained 350 mL of 40 % ible with free acid recovery by distillation (v/v) Alamine 304-1 in Witcohol85 NF, and was replaced every other day. The hollow-fiber mem- [6]. In the present study, this solvent sys- brane extractor consisted of 224 hydrophobie, tem is used in a fed-batch extractive fer- microporous polypropylene hollow fibers mentation with immobilized cells to avoid (Celgard'" X20-400, Hoechst Celanese Corp., product inhibition. Immobilized cells offer Charlotte, NC), each with an effective length of the advantages of high cell densities, elim- 25.4 cm, potted into a glass shell (Iowa State ination of the lag phase, and reduced expo- University Glass Blowing Shop, Ames, lA) with 0.0.,1.0., and length of 14,12.7, and 305 mm, sure to solvent. Fed-batch mode also avoids respectively. The total effective membrane sur- catabolite repression. face area was 716 cm-. Before the fermentation, the shell side of the membrane extractor was chemically sanitized with 500 mL of 3 % (v/v) 2. MATERIALS AND METHODS H202 and then rinsed with 800 mL sterile dei on- ized water.
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