Ethanol stripping by pervaporation using porous PTFE membrane

In a shell-and-tube type of module containing either porous or nonporous tubular membranes, the sweeping action of a flow inert gas in the shell side was used to strip ethanol from an aqueous ethanol solution flowing countercurrently in the tube side. A calculation of the overall mass transfer coefficient, K_G, of the membrane used was made for this system. In ethanol stripping tests using a module containing polytetrafluoreethylene (PTFE) tubular membranes, the K_G was found to be more affected by the liquid flow rate than the gas flow rate. Moreover, the gas side mass transfer coefficient, k_G, was estimated to be about 5×10⁻⁵ mol/cm²·s·atm. The liquid side mass transfer coefficient, k_L, on the other hand, was found to increase linearly with the linear velocity of the aqueous solution. Also, at an average solution temperature range of 21 to 32°C, no significant change in the K_G was observed. Comparison of the K_G of different tubular membranes revealed that the K_G of the PTFE membrane was higher than that of polypropylene or silicone membranes under the given experimental conditions.     

High-titer n-butanol production by clostridium acetobutylicum JB200 in fed-batch fermentation with intermittent gas stripping

Acetone–butanol–ethanol (ABE) fermentation with a hyper‐butanol producing Clostridium acetobutylicum JB200 was studied for its potential to produce a high titer of butanol that can be readily recovered with gas stripping. In batch fermentation without gas stripping, a final butanol concentration of 19.1 g/L was produced from 86.4 g/L glucose consumed in 78 h, and butanol productivity and yield were 0.24 g/L h and 0.21 g/g, respectively. In contrast, when gas stripping was applied intermittently in fed‐batch fermentation, 172 g/L ABE (113.3 g/L butanol, 49.2 g/L acetone, 9.7 g/L ethanol) were produced from 474.9 g/L glucose in six feeding cycles over 326 h. The overall productivity and yield were 0.53 g/L h and 0.36 g/g for ABE and 0.35 g/L h and 0.24 g/g for butanol, respectively. The higher productivity was attributed to the reduced butanol concentration in the fermentation broth by gas stripping that alleviated butanol inhibition, whereas the increased butanol yield could be attributed to the reduced acids accumulation as most acids produced in acidogenesis were reassimilated by cells for ABE production. The intermittent gas stripping produced a highly concentrated condensate containing 195.9 g/L ABE or 150.5 g/L butanol that far exceeded butanol solubility in water. After liquid–liquid demixing or phase separation, a final product containing ～610 g/L butanol, ～40 g/L acetone, ～10 g/L ethanol, and no acids was obtained. Compared to conventional ABE fermentation, the fed‐batch fermentation with intermittent gas stripping has the potential to reduce at least 90% of energy consumption and water usage in n‐butanol production from glucose. Biotechnol. Bioeng. 2012; 109: 2746–2756. © 2012 Wiley Periodicals, Inc.     

Control of packed column fouling in the continuous fermentation and stripping of ethanol

By recycling the contents of a 14 L fermentor through a stripping column to continuously remove ethanol and reduce product inhibition, continuous complete conversion of nutrient feed containing 600 g/L glucose was achieved in a small pilot plant. Ethanol was recovered from the carbon dioxide stripping gas in a refrigerated condenser, and the gas was reheated with steam and recycled by a blower. Productivity of ethanol in the fermentor as high as 15.8 g/L/h and condensate production of up to 10 L/day of almost 50% by volume ethanol were maintained for up to 60 days of continuous operation. Weekly washing of the column packing in situ was required to prevent loss of performance caused by attached growth of yeast cells, which restricts the gas flow rate through the stripping column. (c) 1996 John Wiley & Sons, Inc.     

Systematic errors in data evaluation due to ethanol stripping and water vaporization

Systematic errors due to the neglect of water and/or ethanol partition between liquid and gaseous phases are discussed for bioreactors equipped with or without a condenser. Both water vapor and ethanol vapor are present in the off-gas leaving the condenser. Presence of residual water vapor largely influences the gas measurements by dilution. As a consequence, the oxygen consumption rate can be overestimated by a factor of 3 if calculations are not corrected for water vapor content or if no additional device is implemented after the condenser to completely dry the off-gases. The mass balance and partition equations predict that the condenser has only a small effect on reduction of the ethanol vapor content of the off-gas. The reason is the high ethanol concentration of the condensate droplets on the condenser wall in contact with the off-gases. Model predictions as well as experimental results show that ethanol evaporation represents a large fraction of the ethanol production rate and influences greatly the elemental recoveries. For a reactor working at 30 degrees C without condensation of the vapors and for a volumetric aeration rate of 0.63vvm, stripping of ethanol resulted in a gaseous dilution rate of 0.016 h-1 for ethanol. The dilution rate by stripping was reduced to 0.014 h-1 when a condenser at 12 degrees C was implemented. The fraction of ethanol that is stripped is mainly dependent on the ratio D/vvm (liquid to gaseous flow rates), and the effect is only slightly influenced by low condenser temperature. The evaporation of ethanol may account for more than 20% of the ethanol formation rate. Therefore, the condenser does not succeed to reflux all ethanol to the reactor broth. In terms of a unit operation, ethanol vapor can be efficiently reduced by absorption instead of condensation. To demonstrate the feasibility, a simple modification of the reactor was tested for continuous cultures: the feed port was changed from the top-plate to the top of the condenser, which was used as an absorption column. Ethanol stripping was reduced by a factor of 4 as compared to the condensation setup (at 12 degrees C): it accounted for 2% of the ethanol production rate as compared to 8.2% at D = 0.19 h-1 and 0.63vvm.     

Ethanol production from xylose with the yeast Pichia stipitis and simultaneous product recovery by gas stripping using a gas-lift loop fermentor with attached side-arm (GLSA)

The bioconversion of xylose into ethanol with the yeast Pichia stipitis CBS 5773 is inhibited when 20 g/L of ethanol are present in the fermentation broth. In order to avoid this limitation, the fermentation was carried out with simultaneous recovery of product by CO(2) stripping. The fermentation was also improved by attaching a side-arm to the main body of a classical gas-lift loop fermentor. This side-arm increases the liquid circulation, mass transfer, and gas distribution, reducing the amount of oxygen in the inlet gas necessary to perform the fermentation of xylose under microaerobic conditions (K(L)a approximately 16 h(-1)). The continuous stripping of ethanol from the fermentation broth in this new bioreactor system allowed the consumption of higher xylose concentrations than using Erlenmeyer shaker flasks, improved significantly the process productivity and provided a clean ethanol solution by using an ice-cooled condenser system. Finally, a fed-batch fermentation was carried out with a K(L)a = 15.8 h(-1). Starting with 248.2 g of xylose, 237.6 g of xylose was consumed to produce 88.1 g of ethanol which represents 72.6% of the theoretical yield (47.2 g/L of ethanol was recovered in the condenser, while 9.6 g/L remained in the fermentation broth).     

Formation of ethyl acetate by Kluyveromyces marxianus on whey: studies of the ester stripping

Kluyveromyces marxianus is capable of converting lactose into ethyl acetate offering a chance for an economical reuse of whey. The microbial formation of ethyl acetate as a bulk product calls for an aerobic process and, thus, the highly volatile ethyl acetate is discharged from the aerated bioreactor. This stripping process was modeled and investigated experimentally. The stripping rate was proportional to the gas flow and nearly independent of the stirring rate since the stripping was governed by the absorption capacity of the exhaust gas rather than the phase transfer. Cooling the exhaust gas did not noticeably influence the stripping. One batch experiment is presented in detail to demonstrate the formation of ethyl acetate by K. maxianus DSM 5422 on whey. Further batch experiments showed that a substantial formation of ethyl acetate only occurred when the yeast growth was limited by a lack of trace elements. The highest product yield observed was 0.25 g ethyl acetate per g lactose which is nearly 50% of the theoretical maximum.     

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     

Mixing characteristics and liquid circulation in a new multi-environment bioreactor

The theoretical and experimental aspects of the hydrodynamics and mixing in a new multi-environment bioreactor that uses the air-lift design were investigated. This study focused on the mixing characteristics, residence time distribution, liquid circulation between three zones of aerobic, microaerophilic and anoxic, and liquid displacement in the bioreactor at influent flow rates of 720–1,450 L/day and air flow rates of 15–45 L/min. The theoretical analysis of liquid displacement led to the estimation of the specific rate of liquid discharge from the bioreactor at any given influent flow rate, and the number of liquid circulations between various bioreactor zones before the discharge of a given quantity of wastewater. The ratio of mean residence time to the overall hydraulic retention time (t _m/HRT) decreased with the increase of air flow rate at any given influent flow rate, and approached unity at higher air flow rates. Mixing was characterized in terms of the axial dispersion coefficient and Bodenstein number, demonstrating a linear relationship with the superficial gas velocity. A correlation was developed between the Bodenstein number and the Froude number. The study of liquid circulation between the zones showed that less than 1.5 % of the circulating liquid escapes circulation at each cycle and flows towards the outer clarifier, while the percentage of escaped liquid decreases with increasing air flow rate at a given influent flow rate. The specific rate of liquid discharge from the bioreactor increased from 0.19 to 0.69 h^?1 with the increase of air and influent flow rates from 15 to 45 L/min and 500 to 1,450 L/day, respectively. Under the examined operating conditions, mixed liquor circulates between 364 and 1,698 times between the aerobic, microaerophilic and anoxic zones before 99 % of its original volume is replaced by the influent wastewater.     

Oxygen transfer in liquid-impelled loop reactors using perfluorocarbon liquids

Oxygen transfer in the liquid-impelled loop reactor is described for a setup in which the perfluorochemical FC40 is aerated externally. Two sizes of reactors are investigated. The mass-transfer coefficient k appears to be lower with a factor of about 0.6 compared to gas liquid systems. the specific exchange area in the present experimental setup is found to be favorable when compared with gas liquid bioreactors at the same superficial dispersed-phase velocities. However, slow coalescence of the dispersed-phase drops in the phase separation section limits the dispersed-phase flow rate seriously. In Case this become crucial from the point of view of oxygen supply, special measures need to be found or alternatives such as combined sparging of air and solvent. (c) 1992 John Wiley & Sons, Inc.     

乙醇诱导杂交瘤细胞凋亡的检测

为建立杂交瘤细胞凋亡检测模型,在乙醇诱导下,采用荧光染色、MTT等方法检测H18杂交瘤细胞凋亡时的形态学及增殖活性变化,并用流式细胞仪对其进行定量分析,夹心ELISA检测IgG抗体分泌的变化情况。结果发现5lOmmol／L乙醇作用5～6h的凋亡诱导效果最为明显,在诱导条件下,杂交瘤细胞的活细胞数显著下降,凋亡细胞比例较高。抗体浓度明显下降,与乙醇浓度呈负相关,但与细胞增殖活性无明显的线性关系。故以此为凋亡检测模型,可为后续抗凋亡细胞株的建立与筛选研究提供初步的实验基础,并为乙醇对IgG型抗体分泌的影响研究提供了可能的实验模型。     

Applied in situ product recovery in ABE fermentation

The production of biobutanol is hindered by the product's toxicity to the bacteria, which limits the productivity of the process. In situ product recovery of butanol can improve the productivity by removing the source of inhibition. This paper reviews in situ product recovery techniques applied to the acetone butanol ethanol fermentation in a stirred tank reactor. Methods of in situ recovery include gas stripping, vacuum fermentation, pervaporation, liquid–liquid extraction, perstraction, and adsorption, all of which have been investigated for the acetone, butanol, and ethanol fermentation. All techniques have shown an improvement in substrate utilization, yield, productivity or both. Different fermentation modes favored different techniques. For batch processing gas stripping and pervaporation were most favorable, but in fed‐batch fermentations gas stripping and adsorption were most promising. During continuous processing perstraction appeared to offer the best improvement. The use of hybrid techniques can increase the final product concentration beyond that of single‐stage techniques. Therefore, the selection of an in situ product recovery technique would require comparable information on the energy demand and economics of the process. © 2017 American Institute of Chemical Engineers Biotechnol. Prog., 33:563–579, 2017     

休哈塔假丝酵母乙醇发酵性能的研究

木糖的高效发酵是制约纤维素燃料乙醇生产的技术瓶颈之一,高性能发酵菌种的开发是本领域研究的重点。以木糖发酵的典型菌株休哈塔假丝酵母为材料,研究氮源配比、葡萄糖和木糖初始浓度、葡萄糖添加及典型抑制物等因素对其木糖利用和乙醇发酵性能的影响规律。结果表明,硫酸铵更适宜于木糖和葡萄糖发酵产乙醇。在摇瓶振荡发酵条件下,该酵母可发酵164.0 g/L葡萄糖生成61.9 g/L乙醇,糖利用率和乙醇得率分别为99.8%和74.0%;受酵母细胞膜上转运体系的限制,对木糖的最高发酵浓度为120.0 g/L,可生成45.7 g/L乙醇,糖利用率和乙醇得率分别达到94.8%和87.0%。休哈塔假丝酵母发酵木糖的主要产物为乙醇,仅生成微量的木糖醇;添加葡萄糖可促进木糖的利用;休哈塔假丝酵母在葡萄糖发酵时的乙酸和甲酸的耐受浓度分别为8.32和2.55 g/L,木糖发酵时的乙酸和甲酸的耐受浓度分别为6.28和1.15 g/L。     

Rapid screening of lignans from Phyllanthus myrtifolius and stilbenoids from Syagrus romanzoffiana by HPLC-SPE-NMR

Introduction – Application of on‐line solid‐phase extraction (SPE) as an interface between HPLC and NMR has gained great improvement in solving sensitivity problems and signal interferences by the eluents. Objective – Rapid analysis and characterisation by HPLC‐SPE‐NMR and LC/MS of the arylnaphthalene‐type lignans present in Phyllanthus myrtifolius and the minor stilbenoids present in the polyphenol‐rich fraction from the ethanol extract of the seeds of Syagrus romanzoffiana. Methodology – Pretreatment of fractions by liquid–liquid partitioning, followed by Sephadex LH‐20 fractionation, was found very useful to facilitate the focusing and analysis of the polyphenolic fraction. HPLC‐DAD‐SPE‐NMR (400 MHz and 600 MHz) analysis was carried out using an Agilent 1100 liquid chromatography, followed by a Prospekt 2 automated solid‐phase extraction unit, containing 96 HySphere‐Resin GP cartridges (10 × 2 mm, 10–12 µm), which was connected to a 120 or 60 µL LC probe. Results – Seven arylnaphthalene‐type lignans from the chloroform‐soluble fraction of P. myrtifolius and nine stilbenoids from a polyphenol‐rich butanol‐soluble fraction of the seeds of S. romanzoffiana were characterised. Conclusion – HPLC‐SPE‐NMR associated with HR‐ESI/MS, which consumed only analytical amounts of partially purified mixtures, was demonstrated to be a good tool for rapid screening of both known and new natural products. Copyright © 2011 John Wiley & Sons, Ltd.     

AN IMPROVED STRIPPING TECHNIQUE FOR LIGHTLY ARMORED DINOFLAGELLATES1

Identification of armored heterotrophic dinoflagellates relies, in part, on plate tabulations obtained by SEM. Currently, two methods are used to visualize plate morphology and develop plate tabulations: swelling the sutures between the cellulose plates of intact organisms or stripping off the outer membranes with ethanol to expose the underlying cellulose plates. Both approaches are problematic with lightly armored dinoflagellates because sutures do not consistently swell to enable visualization, and the outer membranes are not consistently stripped. Further, generic and species differences necessitate frequent modification of these protocols to obtain reliable results. We describe an improved membrane stripping technique using the detergent Triton X‐100. Our method provides a more consistent standardized approach to removing the outer membranes of lightly armored dinoflagellates, including Pfiesteria shumwayae Glasgow & Burkholder, a taxon that has, until now, proven very difficult to strip with currently published methods. This method allows visualization of the sulcus, a region previously difficult to observe, and will greatly facilitate taxonomic studies of the lightly armored forms.     

Environmental flow allocations in monsoonal Hong Kong

1. Hong Kong streams are subject to aggressive water extractions but the downstream water needs of ecosystems – i.e. environmental flow (e‐flow) requirements – have not yet been addressed. This study investigated hydro‐ecological relationships that could be used to establish e‐flow allocations for streams in monsoonal Hong Kong. 2. Data were collected during the wet and dry seasons from 10 unpolluted streams experiencing a gradient of flow reductions (c. 0–98%). Relationships between flow conditions (percentage discharge reduction and absolute discharge volume) and responses of macroinvertebrate composition and periphyton condition were established for each season. 3. Declines in richness of Ephemeroptera and abundance of hydropsychid caddisflies, as well as increases in the proportion of predators, were linearly related to percentage discharge reduction during both seasons. Relationships were also recorded for eight other macroinvertebrate richness or compositional metrics during the dry season only. Relationships between macroinvertebrate assemblage attributes and absolute discharge volume across downstream reaches were also evident. Periphyton was relatively insensitive to flow reductions and did not provide useful hydro‐ecological relationships, although declines in autotrophic index were related to percentage discharge reduction during the dry season. 4. Using hydro‐ecological relationships established for macroinvertebrates, two levels of e‐flow were proposed: a ‘threshold’ intended to maintain near‐natural conditions and a ‘degradation limit’ that allowed no more than 25% of the maximum indicator response to flow reduction. Calculated threshold e‐flows required downstream allocation of ≥74% of natural flows; degradation limit e‐flows were ≥12% (wet) and ≥27% (dry). The discharge needed to maintain threshold conditions was 30–105 L s^?1 (wet) and 5–14 L s^?1 (dry), with degradation limit e‐flows of 19–57 L s^?1 (wet) and 3–6 L s^?1 (dry), relative to natural mean discharges of 77–303 L s^?1 (wet) and 3–18 L s^?1 (dry). 5. The proposed e‐flow allocations are indicative only, and significant obstacles to implementation have yet to be surmounted. Any such implementation requires monitoring of outcomes in order to refine the allocations and inform adaptive flow management for Hong Kong streams.     

Actinomycetes scale‐up for the production of the antibacterial,nocathiacin

An Amycolatopsis fastidiosa culture, which produces the nocathiacin class of antibacterial compounds, was scaled up to the 15,000 L working volume. Lower volume pilot fermentations (600, 900, and 1,500 L scale) were conducted to determine process feasibility at the 15,000 L scale. The effects of inoculum volume, impeller tip speed, volumetric gas flow rate, superficial gas velocity, backpressure, and sterilization heat stress were examined to determine optimal scale‐up operating conditions. Inoculum volume (6 vs. 2 vol %) and medium sterilization (R_o of 68 vs. 92 min^?1) had no effect on productivity or titer, and higher impeller tip speeds (2.1 vs. 2.9 m/s) had a slight effect (20% decrease). In contrast, higher backpressure, incorporating increased head pressure at the 15,000 L scale (1.2 vs. 0.7 kg/cm²) and low gas flow rates (0.25 vs. 0.8 vvm), appeared to be problematic (40–50% decrease). High off‐gas CO₂ levels were likely reasons for observed lower productivity. Consequently, air flow rate for this 25‐fold scale‐up (600–15,000 L) was controlled to match off‐gas CO₂ profiles of acceptable smaller scale batches to maintain levels below 0.5%. The 15,000 L‐scale fermentation achieved an expected nocathiacin I titer of 310 mg/L after 7 days. Other on‐line data (i.e., pH, oxygen uptake rate, and CO₂ evolution rate) and off‐line data (i.e., analog production, glucose utilization, ammonium production, and dry cell weight) at the 15,000 L scale also tracked similarly to the smaller scale, demonstrating successful fermentation scale‐up. © 2009 American Institute of Chemical Engineers Biotechnol. Prog., 2009     

Insights into large-scale cell-culture reactors: II. Gas-phase mixing and CO₂ stripping

Most discussions about stirred tank bioreactors for cell cultures focus on liquid-phase motions and neglect the importance of the gas phase for mixing, power input and especially CO(2) stripping. Particularly in large production reactors, CO(2) removal from the culture is known to be a major problem. Here, we show that stripping is mainly affected by the change of the gas composition during the movement of the gas phase through the bioreactor from the sparger system towards the headspace. A mathematical model for CO(2)-stripping and O(2)-mass transfer is presented taking gas-residence times into account. The gas phase is not moving through the reactor in form of a plug flow as often assumed. The model is validated by measurement data. Further measurement results are presented that show how the gas is partly recirculated by the impellers, thus increasing the gas-residence time. The gas-residence times can be measured easily with stimulus-response techniques. The results offer further insights on the gas-residence time distributions in stirred tank reactors.     

Hydrodynamics, mass transfer, and yeast culture performance of a column bioreactor with ejector

A bubble column fitted with an ejector has been tested for its physical and biological performance. The axial diffusion coefficient of the liquid phase in the presence of electrolytes and ethanol was measured by a stimulus-response technique with subsequent evaluation by means of a diffusion model. In contrast to ordinary bubble columns, the coefficient of axial mixing is inversely dependent on the superficial air velocity. The liquid velocity acts in an opposite direction to the backmixing flow in the column. The measurement of volumetric oxygen transfer coefficient in the presence of electrolytes and ethanol was performed using a dynamic gassing-in method adapted for a column. The data were correlated with the superficial air and liquid velocities, total power input, and power for aeration and mixing; the economy coefficient of oxygen transfer was used for finding an optimum ratio of power for aeration and pumping. Growth experiments with Candida utilis on ethanol confirmed some of the above results. Biomass productivity of 2.5 g L(-1) h(-1) testifies about a good transfer capability of the column. Columns fitted with pneumatic and/or hydraulic energy input may be promising for aerobic fermentations considering their mass transfer and mixing characteristics.     

Ethanol production in horizontal bioreactor

Summary The rate of continuous alcohol fermentation by a mixture of free and immobilized yeast cells was found to be higher in a horizontal flow channel reactor than in a vertical column reactor under the same operational conditions. This higher fermentation rate in the horizontal reactor was attributed to accumulation of yeast cells in the reactor by free sedimentation and incomplete mixing in the direction of liquid flow. It was estimated that most of the ethanol in the horizontal bioreactor was produced by free cells in suspended or settled states. The relatively low ethanol production by the immobilized yeast cells on the ethanol production was considered due to higher product inhibition of fermentation rate within the support.