Disintegration of microorganisms in an industrial horizontal mill of novel design

A continuous high-speed horizontal colloid mill of novel design for use in the microbiological and food industries was tested for the disintegration of cells of Saccharomyces cerevisiae and Candida utilis. The mill consists of a horizontal vessel with round or oval cross sections fitted with a high-speed longitudinal agitator shaft on which are mounted disk agitators, alternating radially and obliquely to the shaft. The mill is partly filled with freely moving grinding elements which, during a continuous operation, are maintained in the vessel by a vibrating annular slot separator. Highly efficient cooling is provided by circulation of cooling fluid through a jacket surrounding the vessel as well as through the agitator shaft and disks. The radial agitator disks impart a radial motion to the grinding elements, while the oblique disks give rise to the axial movement of a substantial part of the elements. The crossing of paths thus achieved gives the mill a very high efficiency. Using a mill of 20 liter nominal capacity, the effects of agitator design, agitator speed, flow rate, and concentration of the cell suspension on the disintegration efficiency and heat production were studied. Ninety per cent of S. cerevisiae cells in a 15% suspension could be broken at a residence time of 2.5 min. The temperature rise did not exceed 8° C. The corresponding figure for C. utilis was 84%. The maximal flow rate was 400 liter/hr. Extrapolation indicates that available industrial mills of 300 liter capacity based on the same design can handle flows of 2000 liter/hr.     

Experiences with a 20 litre industrial bead mill for the disruption of microorganisms

Suspensions of several yeast strains and bacterial species were disrupted in a continuously operating industrial agitator mill of 22.7 litre internal working volume. The influence of agitator speed, flow rate, concentration of microorganisms in the slurry, packing density of glass beads and bead diameter on the disruption process was studied using baker's yeast (Saccharomyces cerevisiae). Cell disintegration was followed by assaying the appearance of protein and the activities of d-glucose-6-phosphate dehydrogenase [d-glucose-6-phosphate:NADP⁺ oxidoreductase, EC 1.1.1.49] and α-d-glucosidase [α-d-glucoside glucohydrolase, EC 3.2.1.20] in the soluble fraction. The best operating conditions for the disintegration of baker's yeast with respect to activity yield appeared to be at a rotational speed of 1100 rev/min, a flow rate of 100 litre h^?1 and a cell concentration of 40% (w/v). The location of the desired enzyme in the cell is of importance for the choice of bead diameter and packing density of the glass beads. Temperature increase and power consumption during disintegration are also strongly influenced by the bead loading in the mill. With optimized parameters, 200 kg baker's yeast can be processed per hour with a degree of disintegration >85%. The disruption process in the mill was found to be very effective for several yeast species tested, e.g. Saccharomyces cerevisiae, Saccharomyces carlsbergensis, and Candida boidinii. The usefulness of the Netzsch LME 20-mill for the disruption of bacteria species was demonstrated with Escherichia coli, Brevibacterium ammoniagenes, Bacillus sphaericus and Lactobacillus confusus. As expected, the mill capacity for bacterial disruption was significantly smaller than for the yeast. Between 10 and 20 kg per h bacteria may be processed, depending on the organism.     

Disruption of baker's yeast by a new bead mill

Summary A continuous high-speed bead mill of novel design (Sulzer Annu Mill 01) was tested for cell disruption of baker's yeast as a model system. The efficiency of cell disruption was evaluated for the relative amount of released protein. The effects of rotation speed, cell concentration and flow rate of cell suspension on the cell disruption were investigated. The maximum yield of released protein was found to be 2.62 kg protein/L.h. This novel design appears to be more effective than existing commercially available mills.Notations Cs cell concentration (g packed yeast/L) - F flow rate of suspension, mL/min - F_R cumulative residence time distribution - N rotation speed of the rotor (rpm) - P number of passes of suspension through mill - R amount of protein released from cell, mg/g packed yeast - R_m maximum amount of protein released, mg/g packed yeast - t time, s - mean residence time, s     

Mechanical disintegration of microorganisms in an industrial homogenizer

Disintegration of microorganisms in a continuously working industrial homogenizer has been studied. The homogenizer consists of rotating discs in a cylinder filled with glass beads. Different parameters for disintegration of baker's yeast were investigated. The disintegration process is a first-order reaction and it is influenced by the flow rate of the suspension and by the agitator speed. At a flow rate of 200 liters/hr about 85% of the yeast cells can be disrupted in a single pass through the disintegrator. This type of disintegrator can be used for disruption of cells in order to produce single-cell protein, active enzymes and other valuable cell components.     

A simple method for bakers' yeast cell disruption using a three-phase fluidized bed equipped with an agitator

A three-phase fluidized bed equipped with a turbine agitator was utilized as a simple device for disrupting bakers' yeast cells (Saccharomyces cerevisiae). The degree of yeast cell disruption was evaluated based on the number of broken cells and its validity was confirmed by the total amount of crude soluble proteins released and by microscopic observation. It was found that the equipment could yield 90% of yeast cell disruption. With the presence of glass beads, the degree of cell disruption became higher as agitating speed is increased. The disruption enhancement would be attributed to the grinding effect resulting from the interaction between yeast cells and glass beads. One-thousand micrometers of glass beads yielded a higher degree of disruption than larger ones. An increase in liquid flow rate hindered the degree of disruption because of shorter contact time although the shear rates in the yeast suspension would become more rigorous.     

Reactor properties of a high-speed bead mill for microbial cell rupture

Laboratory and pilot-plant high-speed bead mills of 0.6 and 5 liter capacity and consisting of four and five impellers in series, respectively, were used to follow the batch and continuous disruption of bakers' yeast (Saccharomyces cerevisiae). The mills are not scaled equivalents. Throughputs ranging from 1 × 10^?6m³/sec to 12 × 10^?6m³/sec for the 0.6 liter mill and from 16 × 10^?6m³/sec to 100 × 10^?6m³/sec for the 5 liter mill were used for continuous disruption studies. Variables studied included the effect of impeller tip speed, temperature, and packed yeast concentration (ranging from 15 to75% by weight packed yeast). Disruption kinetics, as measured by the release of soluble protein, followed a first-order rate equation, the rate constant being a function of impeller tip speed and yeast concentration. For continuous disruption studies the bead mills behaved as a series of continuous stirred-tank reactors, each impeller forming a reactor. In the smaller mill a considerable degree of backflow between the reactors was evident. For certain mixing conditions the maximum amount of releasable protein was dependent on the impeller geometry, construction material, and also the concentration of packed yeast. The relative power efficiencies of the two mills are discussed along with possible criteria for scaling of bead mills.     

The disruption ofSaccharomyces cerevisiae cells and release of glucose 6-phosphate dehydrogenase (G6PDH) in a horizontal dyno bead mill operated in continuous recycling mode

Baker’s yeast was disrupted in a 1.4-L stainless steel horizontal bead mill under a continuous recycle mode using 0.3 mm diameter zirconia beads as abrasive. A single pass in continuous mode bead mill operation liberates half of the maximally released protein. The maximum total protein release can only be achieved after passaging the cells 5 times through the disruption chamber. The degree of cell disruption was increased with the increase in feeding rate, but the total protein release was highest at the middle range of feeding rate (45 L/h). The total protein release was increased with an increase in biomass concentration from 10 to 50% (w/v). However, higher heat dissipation as a result of high viscosity of concentrated biomass led to the denaturation of labile protein such as glucose 6-phosphate dehydrogenase (G6PDH). As a result the highest specific activity of G6PDH was achieved at biomass concentration of 20% (ww/v). Generally, the degree of cell disruption and total protein released were increased with an increase in impeller tip speed, but the specific activity of G6PDH was decreased substantially at higher impeller tip speed (14 m/s). Both the degree of cell disruption and total protein release increased, as the bead loading increased from 75 to 85% (v/v). Hence, in order to obtain a higher yield of labile protein such as G6PDH, the yeast cell should not be disrupted at biomass concentration and impeller tip speed higher than 20% (w/v) and 10 m/s, respectively.     

The influence of bakers’ yeast cells on protein adsorption in anion exchange expanded bed chromatography

Baker’s yeast was disrupted in a 1.4-L stainless steel horizontal bead mill under a continuous recycle mode using 0.3 mm diameter zirconia beads as abrasive. A single pass in continuous mode bead mill operation liberates half of the maximally released protein. The maximum total protein release can only be achieved after passaging the cells 5 times through the disruption chamber. The degree of cell disruption was increased with the increase in feeding rate, but the total protein release was highest at the middle range of feeding rate (45 L/h). The total protein release was increased with an increase in biomass concentration from 10 to 50% (w/v). However, higher heat dissipation as a result of high viscosity of concentrated biomass led to the denaturation of labile protein such as glucose 6-phosphate dehydrogenase (G6PDH). As a result the highest specific activity of G6PDH was achieved at biomass concentration of 20% (ww/v). Generally, the degree of cell disruption and total protein released were increased with an increase in impeller tip speed, but the specific activity of G6PDH was decreased substantially at higher impeller tip speed (14 m/s). Both the degree of cell disruption and total protein release increased, as the bead loading increased from 75 to 85% (v/v). Hence, in order to obtain a higher yield of labile protein such as G6PDH, the yeast cell should not be disrupted at biomass concentration and impeller tip speed higher than 20% (w/v) and 10 m/s, respectively.     

Influence of processing parameters on disintegration of Chlorella cells in various types of homogenizers

The following bead mills used for disruption of the microalga Chlorella cells were tested: (1) Dyno-Mill ECM-Pilot, grinding chamber volume 1.5 L; KDL-Pilot A, chamber volume 1.4 L; KD 20 S, chamber volume 18.3 L; KD 25 S, chamber volume 26 L of Willy A. Bachofen, Basel, Switzerland, (2) LabStar LS 1, chamber volume 0.6 L of Netzsch, Selb, Germany, (3) MS 18, chamber volume 1.1 L of FrymaKoruma, Neuenburg, Germany. Amount of disrupted cells decreased with increasing Chlorella suspension feed rate and increased up to about 85% of the beads volume in the grinding chamber of the homogenizers. It also increased with agitator speed and number of passes of the algae suspension through the chamber. The optimum beads diameter was 0.3–0.5 mm in the homogenizers Dyno-Mill and LabStar LS 1 and 0.5–0.7 mm in the homogenizer MS 18. While the degree of the cell disruption decreased with increasing cell density in Dyno-Mill and LabStar, the cell disruption in the MS 18 increased. Depending on processing parameters, more than 90% of algae cells were disrupted by passing through the bead mills and bacteria count in algae suspension was reduced to about two orders.     

Experimental study of microorganism disruption using shear stress

There has been a broad spectrum of theoretical and experimental works on microorganism disruption methods undertaken in the past. However, there is a lack of understanding regarding the actual reasons for microorganism disruption using ultrasound and whether it is caused by shock or shear. In the case of shear stress, which is the focus of this paper, analysis of the intense turbulent flow region of an in-house built shear apparatus combined with the experimental results demonstrated that when the energy dissipation rate in the turbulence region is high, and the size of the eddy is smaller than the size of the cell, the likelihood of yeast disruption is high. The mechanical properties of yeast cells combined with the calculated energy dissipation rate were used to evaluate the yeast disruption efficiency (log reduction). The results show that the shear apparatus can efficiently and effectively disrupt S. cerevisiae at different treatment times, suspension temperatures and rotor speeds. The experimental work suggests that maximum yeast log reduction was achieved when the maximum power dissipation of 2.095 kW was recorded at 10,000 RPM, while suspension temperature was controlled below 35 °C. The corresponding shear stress at 10,000 RPM was 2586.2 Pa.     

A rapid method for determination of acid phosphatase activity of whole yeast cells

A simple and rapid procedure for determination of intracellular acid phosphatase activity without the need for disruption of cells is described. Candida lipolytica cell suspension was treated with 0.1% Triton X-100 for 30 min at room temperature and with intermittent shaking. The enzyme assay is carried out directly with the permeabilized cell suspension. Permeabilization of the yeast cells to p -nitrophenylphosphate by Triton X-100 provides almost 100% efficiency in determining the total acid phosphatase activity compared to results obtained with disrupted yeast cells.     

Separation of yeast cells from aqueous solutions using magnetically stabilized fluidized beds

AIMS: To separate Saccharomyces cerevisiae cells from aqueous solutions using magnetically stabilized fluidized beds (MSFB) that utilize a horizontal magnetic field, and to study the effect of some parameters, such as bed porosity and height, liquid flow rate and inlet concentration on cell removal efficiency and breakthrough curves. METHODS AND RESULTS: The separation process was conducted in an MSFB under the effect of horizontal magnetic field. The magnetic particles used consist of a ferromagnetic core of magnetite (Fe3O4) covered by a stable layer of activated carbon to adsorb the yeast cells from the suspension. The yeast cell concentration in the effluent was determined periodically by measuring the absorbance at 610 nm. The effect of the magnetic field intensity on the bed porosity and consequently the exit-normalized cell concentration from the bed was studied. It was found that bed porosity increased by 75%, and the normalized cell concentration in the bed effluent decreased by 30%, when the magnetic field intensity was increased from 0 to 110 mT. In addition, increasing the magnetic field intensity and bed height delayed the breakthrough point, and allowed efficient cell removal. These results demonstrate an improved method to separate cells of low concentration from cell suspension. CONCLUSIONS: This study allows the continuous separation of yeast cells from aqueous solutions in an MSFB. The removal efficiency is affected by different parameters including the bed height, flow rate and initial concentration. The removal efficiency reaches 82%, and could be improved by varying the operational parameters. SIGNIFICANCE AND IMPACT OF THE STUDY: The results obtained in this investigation show that the MSFB using horizontal fields represents a potential tool for the continuous separation of cell suspension from aqueous solution. This study will contribute to a better understanding of the hydrodynamic parameters on the separation efficiencies of the cell.     

Effects of colloidal fouling and gas sparging on microfiltration of yeast suspension

Cross-flow microfiltration is an important step in separating Baker’s yeast (Saccharomyces cerevisiae) from aqueous suspension in many processes. However the permeate flux often declines rapidly due to colloidal fouling of membranes and concentration polarisation. The present work explores the possibility of maintaining acceptable permeate flux by co-current sparging of gas along with the feed, which would scour away colloidal deposits and reduce concentration polarisation of membranes. In this work, both washed and unwashed yeast were used to study the effect of washing to reduce protein fouling of membranes. It was found that permeate flux increased by 45% for liquid throughput of 75 kg/h for a feed concentration of 2.0 kg/m³ of washed yeast as compared with unwashed yeast suspension without gas sparging. For washed yeast suspension, the increase in gas flow rate from 0.5 lpm to 1.5 lpm (30 l/h to 90 l/h) had beneficial effect on permeate flux. It is concluded that in the present case, the gas flow rate should be less than or equal to the liquid flow rate for enhancement of permeates flux.     

Kinetic analysis of disruption of excess activated sludge by Dyno Mill and characteristics of protein release for recovery of useful materials

Solubilization of excess sludge (ES) cultivated in a laboratory and that obtained from real wastewater treatment plants by continuous Dyno Mill disruption were studied for the purpose of effective reuse of ES. The total soluble protein concentration released during the ES disruption was found to be closely dependent upon the released protease activity, which suggests the possibility of the enzyme recovery as one of the ES reuse methods. The operating parameters of Dyno Mill significantly affected the ES solubilization. A high ES solubilization ratio of about 53%, defined by soluble TOC per total carbon contained in the laboratory-cultivated ES, was achieved by using glass beads of 0.5mm in diameter with the 60% (v/v) bead loading at the disc agitating speed of 3200rpm. The ES solubilization by the continuous mill disruption was successfully analyzed by a kinetic model consisting of first-order disruption kinetics. The collision frequency between the moving beads correlated well with the ES solubilization rate constant under all the operating conditions. This study proposes the applicability of mill disruption to the ES solubilization and to its reuse process.     

Improved cell disruption of Pichia pastoris utilizing aminopropyl magnesium phyllosilicate (AMP) clay

An efficient method for Pichia cell disruption that employs an aminopropyl magnesium phyllosilicate (AMP) clay-assisted glass beads mill is presented. AMP clay is functionalized nanocomposite resembling the talc parent structure Si₈Mg₆O₂₀(OH)₄ that has been proven to permeate the bacterial membrane and cause cell lysis. The recombinant capsid protein of cowpea chlorotic mottle virus (CCMV) expressed in Pichia pastoris GS115 was used as demonstration system for their ability of self-assembly into icosahedral virus-like particles (VLPs). The total protein concentration reached 4.24 mg/ml after 4 min treatment by glass beads mill combined with 0.2 % AMP clay, which was 11.2 % higher compared to glass beads mill only and the time was half shortened. The stability of purified CCMV VLPs illustrated AMP clay had no influence on virus assembly process. Considering the tiny amount added and simple approach of AMP clay, it could be a reliable method for yeast cell disruption.     

Integration of mechanical cell disruption and fluidised bed recovery of G3PDH from unclarified disrupted yeast: a comparative study of the performance of unshielded and polymer shielded dye-ligand chromatography systems

The development of a simplified process for the simultaneous disruption and direct selective purification of intracellular proteins from unclarified yeast disruptate has been investigated. The recovery of glyceraldehyde 3-phosphate dehydrogenase (G3PDH) from baker's yeast was selected as a potential demonstration of the generic applicability and practical feasibility of this integrated technique. The application of an adsorbent characterised by high density (UpFront steel-agarose; rho=2.65g ml(-1)) facilitated the combining of cell disruption operation (bead milling of 50% ww/v of yeast suspension at 7.2 lh(-1)) with fluidised bed dye-ligand (Cibacron Blue 3GA) adsorption operated immediately downstream of the disrupter. The adoption of a polymer shielded, dye-ligand technique advanced recovery efficiency. It was demonstrated that G3PDH could be recovered with a yield of 67.5% bound activity and a specific activity of 40.2IU mg(-1), after a single step elution with 0.15M NaCl. The generic application of this approach has been evaluated.     

Enhancement of display efficiency in yeast display system by vector engineering and gene disruption

Vector engineering and gene disruption in host cells were attempted for the enhancement of α-agglutinin-based display of proteins on the cell surface in yeast. To evaluate the display efficiency by flow cytometric analysis, DsRed-monomer fused with FLAG-tag was displayed and immunostained as a model protein. The use of leu2-d in the expression vector resulted in the enhanced efficiency and ratio of the accessible display of proteins. Moreover, the amount of displayed proteins in SED1-disrupted cells increased particularly during the stationary growth phase. The combination of these improvements resulted in the quantitatively enhanced accessible display of DsRed-monomer on the yeast cell surface. The improved yeast display system would be useful in a wider range of its applications in biotechnology.     

Effects of the N-Substitution and Physical Form of Chitosan and the Modification of its Nonreducing End Groups on the Rates of Hydrolysis by Chitinase from Streptomyces griseus

Zymolyase was purified from Zymolyase-60,000 by ion-exchange chromatography with sugar and gel filtration. Zymolyase was separated into the two protein fractions A and B. Neither alone could lyse yeast cells, but together showed high lytic activity. Zymolyase A and B were β-1,3-glucanase and alkaline protease, respectively. On stepwise treatment of yeast cells with the enzymes, yeast cells were lysed only by treatment with Zymolyase A after pretreatment with Zymolyase B. Zymolyase A lysed yeast cells in the presence of 2-mercaptoethanol, but B could not even at high concentration. Zymolyase B decreased the turbidity of a yeast cell suspension by about 13%.     

Degradation of waste waters from olive oil mills by Yarrowia lipolytica ATCC 20255 and Pseudomonas putida

Waste waters from olive oil processing may cause severe pollution in the Mediterranean area, since they have a high level of chemical oxygen demand (COD) (100–200 g/l) and contain other organic and inorganic compounds. In all olive oil producing countries, the reduction of pollution in olive oil mill waste waters at reasonable costs and using techniques suitable for most industrial applications is an unsolved problem. For this paper, the yeast Yarrowia lipolytica ATCC 20255 was grown on waste waters from an olive oil mill in a 3.5 1 fermenter under batch culture conditions. The results showed that the yeast was capable of reducing the COD value by 80% in 24 h. In this way, a useful biomass of 22.45 g/l as single cell protein (SCP) and enzyme lipase were produced. During this process, most of the organic and inorganic substances were consumed, only aromatic pollutants were still present in the fermentation effluents. Therefore, we used a phenol degrader, namely Pseudomonas putida, to reduce phenolic compounds in the fermentation effuents after removing Yarrowia lipolytica cells. P. putida was effective in reducing phenols in only 12 h.     

A microscale bacterial cell disruption technique as first step for automated and miniaturized process development

Cell disruption is crucial during recovery of biopharmaceuticals overexpressed in E. coli, which tend to be produced intracellularly as insoluble inclusion bodies. Miniaturized high-throughput systems can accelerate the laborious downstream protocol for such biopharmaceuticals and enable integrated process-development. A fast and robust cell disruption method reflecting the protein and impurity profile of homogenates obtained by large-scale methods is required for such an approach. We established a miniaturized bead mill for parallel mechanical cell disruption at the microscale. Its total protein and impurity release, protein pattern, and particle size distribution were compared to results from microscale enzymatic digestion and referred to laboratory-scale high-pressure homogenization. Bead mill disruption led to equivalent protein and impurity release as well as to the same particle size profile as the large-scale reference. In contrast, lysates obtained by enzymatic digestion contained only 30–47% of overall protein, 17% of dsDNA, and 7–10% of endotoxin compared to those obtained by high-pressure homogenization; also larger debris was present in lysates after enzymatic digestion. The established method is fast, efficient, robust and comparable to current large-scale standards, allowing for parallelization of experiments. Thus, it is the method of choice for rapid integrated process development at the microscale.