Economic evaluation of a multicompartment bioreactor for ethanol production usingIn Situ extraction of ethanol

Applied Biochemistry and Biotechnology - We have previously described a multicompartment reactor that can be used with yeast (Saccharomyces cerevisiae) for ethanol production from a starch...     

Improvement of ethanol selectivity of silicalite membrane in pervaporation by silicone rubber coating

In order to improve the pervaporation performance of silicalite membrane, two types of silicone rubber, KE45 and KE108, were coated on the membrane surface. The initial molecular weight of KE108 is high and vulcanizing starts when it comes into contact with moisture in air, whereas the initial molecular weight of KE45 is low and vulcanizing starts when it is mixed with a catalyst. KE108 was found to be more effective than KE45 in enhancing the ethanol selectivity of silicalite membranes. A membrane coated using a 3 wt.% KE108 hexane solution showed separation factor of =125 with a total flux of 0.14 kg/m² h.     

Recovery of pyridine from aqueous solution by membrane pervaporation

Three different membranes, based on poly(dimethylsiloxane) (PDMS), cation-exchange material and poly(vinyl alcohol) (PVA) respectively, were tudied for the separation of pyridine-water mixtures by pervaporation. The PDMS membrane was preferentially permeable to pyridine and the other two were selective towards water. Three membranes showed different permeation performance, allowing the application of the technique to the separation of feeds of different composition. The temperature profile of the permeability suggests that it is possible to carry out the operation at an elevated temperature in order to achieve high productivity. A combination of the three types of membranes was designed for the production of anhydrous pyridine from dilute pyridine aqueous solution by pervaporation.     

Development of a total analytical system by interfacing membrane extraction, pervaporation and high-performance liquid chromatography

This paper discusses the interfacing of continuous membrane extraction, pervaporation and on-line HPLC-UV detection into a total analytical system (TAS). Organics from a water sample were extracted into an organic solvent, and then concentrated via pervaporation prior to HPLC-UV detection. Factors affecting the system performance were studied. With optimized experimental parameters enrichment factors as high as 192 were obtained, the method detection limits were at low ng/mL levels, and the precisions were better than 5%.     

Dehydration of tetrahydrofuran by pervaporation using a composite membrane

Tetrahydrofuran (THF) is a strong aprotic solvent, commonly used in the pharmaceuticals industry due to its broad solvency for both polar and non-polar compounds. THF and water form a homogeneous azeotrope at 5.3 wt.% water thus simple distillation is not feasible to dehydrate THF below this concentration. Pervaporation offers a solution since it is not governed by vapour–liquid equilibria. However many polymer-based pervaporation membranes are cast utilizing THF as the casting solvent and so these membranes have a tendency to swell excessively in its presence. This results in poor separation performance and poor long-term stability and thus renders these membranes unsuitable for THF dehydration.In this study, a new membrane available from CM Celfa, CMC-VP-31 has been tested for the dehydration of THF. The membrane shows excellent performance when dehydrating THF with a flux of over 4 kg m⁻² h⁻¹ when dehydrating THF containing 10 wt.% water at 55 °C dropping to 0.12 kg m⁻² h⁻¹ at a water content of 0.3 wt.%. The permeances of water and THF in the membrane were calculated to be 11.76 × 10⁻⁶ and 7.36 × 10⁻⁸ mol m⁻² s⁻¹ Pa⁻¹, respectively, at 25 °C and found to decrease in the membrane with increasing temperature to values of 6.71 × 10⁻⁶ and 1.63 × 10⁻⁸ mol m⁻² s⁻¹ Pa⁻¹ at 55 °C. The flux and separation factor were both found to increase with an increase in temperature thus favouring the operation of CMC-VP-31 at high temperatures to optimize separation performance.     

Continuous process for singlet oxygenation of hydrophobic substrates in microemulsion using a pervaporation membrane

Chemically generated singlet oxygen (1O2, 1Deltag) is able to oxidize a great deal of hydrophobic substrates from molybdate-catalyzed hydrogen peroxide decomposition, provided a suitable reaction medium such as a microemulsion system is used. However, high substrate concentrations or poorly reactive organics require large amounts of H2O2 that generate high amounts of water and thus destabilize the system. We report results obtained on combining dark singlet oxygenation of hydrophobic substrates in microemulsions with a pervaporation membrane process. To avoid composition alterations after addition of H2O2 during the peroxidation, the reaction mixture circulates through a ceramic membrane module that enables a partial and selective dewatering of the microemulsion. Optimization phase diagrams of sodium molybdate/water/alcohol/anionic surfactant/organic solvent have been elaborated to maximize the catalyst concentration and therefore the reaction rate. The membrane selectivity towards the mixture constituents has been investigated showing that a high retention is observed for the catalyst, for organic solvents and hydrophobic substrates, but not for n-propanol (cosurfactant) and water. The efficiency of such a process is illustrated with the peroxidation of a poorly reactive substrate, viz., beta-pinene.     

Polymeric membrane pervaporation

Pervaporation is an efficient membrane process for liquid separation. The past decades had witnessed substantial progress and exciting breakthroughs in both the fundamental and application aspect of pervaporation. This review provided an analytical overview on the potential of pervaporation for separating liquid mixtures in terms of the solubility parameter and the kinetic parameter of solvents. Focus of the review was given to the fundamental understanding of the membrane. Research progress, challenges and opportunities, and the prospect of pervaporation were also discussed. The thermodynamic approach of pervaporation, featuring emphasizing membrane/species interactions, though gained great successes in the past decades, is now facing its toughest challenge in the org–org separation. A kinetic era of pervaporation, featuring emphasizing diffusion selectivity, as well as the synergy between the selective diffusion and sorption, is in the making, and this approach will eventually find solutions to the challenging org–org separation.     

Treatment of effluents from a membrane bioreactor by nanofiltration using tubular membranes

Production of bioproducts is associated with the generation of considerable amounts of effluents from the bioreactors used. Application of the nanofiltration process was proposed for the treatment of these effluents in order to separate both inorganic and organic solutes. Composition of the fermentation broth precludes the utilization of traditional spiral-wound modules (high turbidity) for the solutes separation in the NF process. The tubular module with AFC30 membranes applied in this work enables such a possibility. Transport and separation characteristics of the NF membrane were determined for the reference solutions containing components present in the effluents generated during the fermentation of glycerol with the use of bacteria.     

Evaluation of PTMSP membranes in achieving enhanced ethanol removal from fermentations by pervaporation

The use of membrane processes for the recovery of fermentation products has been gaining increased acceptance in recent years. Pervaporation has been studied in the past as a process for simultaneous fermentation and recovery of volatile products such as ethanol and butanol. However, membrane fouling and low permeate fluxes have imposed limitations on the effectiveness of the process. In this study, we characterize the performance of a substituted polyacetylene membrane, poly[(l-trimethylsilyl)-l-propyne] (PTMSP), in the recovery of ethanol from aqueous mixtures and fermentation broths. Pervaporation using PTMSP membranes shows a distinct advantage over conventional poly(dimethyl siloxane) (PDMS) membranes in ethanol removal. The flux with PTMSP is about threefold higher and the concentration factor is about twofold higher than the corresponding performance achieved with PDMS under similar conditions. The performance of PTMSP with fermentation broths shows a reduction in both flux and concentration factor relative to ethanol-water mixtures. However, the PTMSP membranes indicate initial promise of increased fouling resistance in operation with cell-containing fermentation broths.     

Continuous direct solvent extraction of butanol in a fermenting fluidized-bed bioreactor with immobilizedClostridium acetobutylicum

Applied Biochemistry and Biotechnology - ImmobilizedClostridium acetobutylicum was used to ferment glucose into acetone and butanol in a fluidized-bed bioreactor. A nontoxic immiscible solvent,...     

The effect of membrane module configuration on extraction efficiency in an extractive membrane bioreactor

The extractive membrane bioreactor (EMB) is a new technology for the treatment of wastewaters containing poorly water-soluble organic compounds. It consists of a bioreactor linked to membrane modules which contain bundles of silicone rubber tubes. Wastewater is pumped through the tube lumens and the biomedium is circulated around the shell side. This paper describes two simple mathematical models developed to compare EMB flow configurations and the results of experiments performed to test the models. We show that tube side Reynolds number has a significant effect on the mass-transfer coefficient of the test pollutant (monochlorobenzene) through the membrane. We also show that, on scale up, for a constant wastewater membrane residence time, an EMB consisting of three membrane modules with tube side recycle flows ≈40 times the wastewaster flow will have a higher extraction efficiency than an equivalent EMB with plug flow inside the module.     

EPDM as a selective membrane material in pervaporation

Various types of ethylene–propylene-diene terpolymers (EPDM) and crosslinking procedures have been investigated with pervaporation, vapor sorption, liquid sorption and gas permeation experiments. The EPDM parameters that have been changed are ethylene content, molecular weight, choice of third monomer, type of branching and various crosslinking procedures.The permeability coefficients were determined from pervaporation experiments and were about 40,000 Barrer for toluene and 700 Barrer for water. However, from vapor sorption measurements, a value of 22,000 Barrer for toluene was obtained which is somewhat lower. It should be realized that these data can only be compared qualitatively; the permeabilities obtained from sorption isotherms are derived data while in case of the pervaporation experiments it is experimentally measured.There is an indication that toluene behaves independently from water but the presence of toluene does influence the water flux during pervaporation. Gas permeation experiments resulted in permeabilities for CO₂, O₂ and N₂ of 120, 24 and 11 Barrer, respectively. No clear differences were found for both EPDM-variation and different crosslinking procedures.     

Ethanol production in a membrane bioreactor

Pilot plant trials were conducted in a corn wet mill with a 7000-L membrane recycle bioreactor (MRB) that integrated ceramic microfiltration membranes in a semi-closed loop configuration with a stirred-tank reactor. Residence times of 7.5–10 h with ethanol outputs of 10–11.5% (v/v) were obtained when the cell concentration was 60–100 g/L drywt of yeast, equivalent to about 10⁹−10¹⁰ cells/mL. The performance of the membrane was dependent on the startup mode and pressure management techniques. A steady flux of 70 L/(m²·h) could be maintained for several days before cleaning was necessary. The benefits of the MRB include better productivity; a clear productstream containing no particulates or yeast cells, which should improve subsequent stripping and distillation operations; and substantially reduced stillage handling. The capital cost of the MRB is $21–$34/(m³·yr) ($0.08–$0.13/[gal·yr]) of ethanol capacity. Operating cost, including depreciation, energy, membrane replacement, maintenance, labor, and cleaning, is $4.5–9/m³ ($0.017–$0.034/gal) of ethanol.     

Characteristics of aerobic biogranules from membrane bioreactor system

As a novel membrane bioreactor (MBR) system, membrane granular sludge bioreactor (called MGSBR) had not only good performance of pollutant degradation in synthetic wastewater, but also alleviated membrane fouling. The study on the stability of aerobic biogranules followed the investigation of MGSBR performance will pay more attraction and potential to this technology during the wastewater treatment in the future. Although the granules had smaller average diameter, poorer settleability and of a sort sludge activity with 2.0 mm of the average diameter, 70 ± 10 mL gSS⁻¹ of SVI and 0.83 of VSS/SS ratio, respectively, the results presented in this paper demonstrated that some characteristics of aerobic biogranules in MGSBR system were ultimately preserved. Changes in characteristics of aerobic biogranules were more or less associated with the overgrowth of filamentous bacteria (showed by SEM observation), which was a phenomenon occurred under the combined effects of continuous aeration mode, reduced DO concentration, long SRT and high EPS concentration in MGSBR. Much research should be performed in the future to control the overgrowth of filamentous bacteria in MGSBR system.     

Operability and feasibility of ethanol production by immobilizedZymomonas mobilis in a fluidized-bed bioreactor

Studies have been carried out using immobilized Z.mobilis in fluidized-bed bioreactors and have emphasized operation during high productivity and conversion. The bacteria are immobilized within small uniform beads (~1 to 1.5-mm diam) of K-carrageenan at cell loadings of 15-50 g (dry wt)/L. Conversion and productivity were measured under a variety of conditions, including feedstocks, flow rates, temperature, pH, and column sizes (up to 2.5 m tall). Volumetric productivities of 50-120 g EtOH/h-L reactor volume have been achieved. Productivities of 60 g/h-L are demonstrated from a 15% feed with residual glucose concentrations of less than 0.1% and 7.4% EtOH in the tallest fermentor. Among feeds of 10, 15, and 20% dextrose, the 15% gave the highest productivity and avoided substrate inhibition. A temperature of 30°C and pH 5 were the optimum conditions. The ethanol yield was shown to be nearly constant at 0.49 g EtOH/g glucose, or 97% of the theoretical under a variety of conditions and transients. The biocatalyst beads have been shown to remain active for two months. Nonsterile feed has been used for weeks without detrimental contamination. The advantages of this advanced bioreactor system over conventional batch technology are discussed.     

Separation of acetic acid-water mixtures by pervaporation through silicalite membrane

Polycrystalline silicalite membranes were prepared on two kinds of porous supports by hydrothermal synthesis. The pervaporation performance of the silicalite membrane obtained was investigated using an acetic acid-water mixture as a feed. The silicalite membrane on the sintered stainless steel support selectively permeates acetic acid in the concentration of the feed acetic acid in the region of 5 to 40 vol%. However, the membrane on the porous alumina support showed no separation for the aqueous acetic acid solution. From the fact that the top layer of the membrane on the alumina support was not composed of pure silicalite but ZSM-5 zeolite crystals, which contained Brønsted acidic sites (Si(OH)Al) in the framework, it was suggested that the acidic sites associated with the framework aluminums play an important role in the separation of the acetic acid-water mixture. A long-term test of the pervaporation was also carried out to clarify the stability of the membrane.     

Continuous flow liquid membrane extraction: a novel automatic trace-enrichment technique based on continuous flow liquid-liquid extraction combined with supported liquid membrane

Combining the continuous flow liquid-liquid extraction (CFLLE) and supported liquid membrane (SLM) extraction, a novel aqueous-aqueous extraction technique that we termed continuous flow liquid membrane extraction (CFLME) is developed for trace-enrichment. The analyte was firstly extracted into the organic phase in the CFLLE step, then transported onto the organic liquid membrane that formed on the surface of the micro porous membrane of the SLM equipment. Finally, it passed through the liquid membrane and was trapped by the acceptor. Aspects related to CFLME were studied by using dichloromethane as liquid membrane, and sulfonylurea herbicides as model compounds. An enrichment factor of over 1000 was obtained when 10 μg l⁻¹ of MSM was enriched for 120 min by this technique. The drawbacks of only a few organic solvents can be selected as liquid membrane with a limited lifetime in SLM operation was overcome. In this CFLME method, almost all solvents that used in the conventional liquid-liquid extraction (LLE) can be adopted and the lifetime of liquid membrane is no longer a problem.     

Continuous production of succinic acid by a fumarate-reducing bacterium immobilized in a hollow-fiber bioreactor

Enterococcus faecalis RKY1, a fumarate-reducing bacterium, was immobilized in an asymmetric hollow-fiber bioreactor (HFBR) for the continuous production of succinic acid. The cells were inoculated into the shell side of the HFBR, which was operated in transverse mode. Since the pH values in the HFBR declined during continuous operation to about 5.7, it was necessary to change the feed pH from 7.0 to 8.0 after 24 h of operation in order to enhance production of succinic acid. During continuous operation with a medium containing fumarate and glycerol, the productivity of succinate was 3.0–10.9 g/(L·h) with an initial concentration of 30 g/L of fumarate, 4.9–14.9 g/(L·h) with 50 g/L of fumarate, and 7.2–17.1 g/(L·h) with 80 g/L of fumarate for dilution rates between 0.1 and 0.4 h⁻¹. The maximum productivity of succinate obtained by the HFBR (17.1 g of succinate /[L·h]) was 1.7 times higher than that of the batch bioconversions (9.9 g of succinate /[L·h]) with 80 g/L of fumarate. Furthermore, the long-term stability of the HFBR was demonstrated with a continuously efficient production of succinate for more than 15 d (360 h).     

Continuous, on-line monitoring of haloacetic acids via membrane extraction

Haloacetic acids are an important class of disinfection byproducts that are being regulated. In this paper we report novel instrumentation for continuous monitoring of the nine haloacetic acids. Hollow fiber liquid-liquid membrane extraction (LLME) and supported liquid membrane extraction (SLME) followed by on-line HPLC-UV detection were studied. With continuous LLME, seven halo-acetic acids could be analyzed and enrichment factor (EF) was around 50. All the nine acids could be extracted and quantified by continuous SLME. Experiments with laboratory standards demonstrated that EF and extraction efficiency could be as high as 500 and 54%, respectively. Relative standard deviations based on seven replicates were between 3.3 and 10.3%, and the MDLs were at sub-ppb levels.