METHOD OF PREPARING A YEAST-CELL LYTIC ENZYME SYSTEM

Abstract: Continuous method for preparing a yeast cell lytic enzyme system having desired beta (1 - 3) glucanase and protease activities. A suitable bacterium which produces the lytic enzyme system is inoculated onto an appropriate growth medium containing predetermined amounts of a carbon source (for example, sugar) and an inducer of lytic enzyme activity. The bacterium is continuously fermented aerobically, the dilution rate being varied to obtain the desired beta (1 - 3) glucanase and protease activities. The bacterium may be one or more of the group consisting of Cytophaga, Oerskovia or Arthrobacter.

Description: METHOD OF PREPARING A YEAST-CELL LYTIC BKZYMB SYSTEM ' Background of the Invention This invention is a method for preparing a yeast cell lytic enzyme system having desired beta (l-»3) glucanase and protease activities. The method provides an effi¬ cient and continuous way to synthesize a lytic enzyme system. Yeast cell walls consist of two layers. The outer layer is a mannan-protein complex and the inner layer is an al ali-insoluble glucan. To break the wall the presence of both glucanase and protease enzymes are necessary. Only small amounts of protease seem to be required. To break brewer's yeast cells, glucanase displays more profound lytic action than the lytic enzyme (glucanase and protease) alone after a brief treatment of the cells with lytic enzyme. The protease appears to be important in the initial attack on the cell surface. The opening of polypeptide chains by the protease makes the inner glucan layer of the wall ac¬ cessible to the glucanase. Yeast cell lytic enzyme systems may be produced by either batch or continuous fermentation. The continu¬ ous process is superior to the batch process with re¬ gard to enzyme production. Furthermore, the composi¬ tion (constituent enzymes) of the lytic enzyme systems can be manipulated by the use of different inducers and by altering the dilution rate. The existence of lytic enzyme systems with different component activities has a potential for their use in specialized applications. Such applications include production of food grade protein and intracellular enzymes, isolation of intracellular recombinant protein produced in yeast, digestion of cell wall polysaccharides, production of protoplasts, as anticaries agents, in the study of cell wall structure, in the treatment of fungal diseases and as an essential tool for cell fusion, transforma- tion and genetic engineering of yeast. GB 1,048,887 discloses a process for producing an en¬ zyme complex having strong proteolytic activity. The organism used to produce this enzyme complex is a spe- cies of the genus Cytophaga. Media compositions and conditions are described for culturing Cytophaga NCIB 9497 in a batch system. Centrifugation of the crude product of the culture and precipitation from aqueous solution with a protein precipitant are described as methods of recovery. GB 1,179,935 discloses a process for producing cytoly- tic enzymes which are capable of lysing the living cells of microorganisms. The system is a batch fermen- tation of Cytophaga johnsonii as well as other species of the genus Cytophaga. GB 1,186,998 discloses another process for producing cytolytic enzymes of microorganisms in a batch fermen- tation. The presence of cells of other microorganisms or decomposites thereof in the nutrient medium results in accelerated production of the cytolytic enzymes. ytop aga johnsonii as well as other Cytophagas may be cultured under the disclosed invention. US 3,716,452 discloses an enzyme for lysing yeast cell walls. The enzyme is produced in a batch fermentation of microorganisms belonging to Arthrobactgr luteus nov.sp. The enzyme has activity for lysing cell walls of yeast dead or alive and at any stage of growth. Lilley, et al. (J. appl. Chem. Biotechnology, vol. 24, pp. 677-686, (1974)) describe continuous-flow cultiva¬ tion of a thermophilic streptomycete in a medium con¬ taining glycerol as the principal carbon source. Lev- els of beta (l-»3) glucanase in the fermentation broth increased sharply as the dilution rate was decreased below 0.20 h "1 . Obata, et al. (J. Ferment. Technol., vol. 53, no. 5, pp. 256-263, (1975)) describe culture conditions for batch production of yeast lytic enzymes from Oerskovia sp. ck. The culture filtrate exhibited high lytic activity toward cells of many species of yeast when the yeast cells were used as substrate. In particular, it was found that glucan, the main component of yeast cell wall, and laminarin (which has a structure similar to glucan) were effective inducers. Beta (l-*3) glucanase and protease were two of several enzymes produced. Rowley and Bull (Biotechnology and Bioengineering, vol. 19, pp. 879-899 (1977)) describe the production of lytic enzyme complex in batch and continuous-flow fer- enters using a yeast-lyzing Arthrobacter species. In growth medium containing whole yeast cells as inducers, an extracellular lytic enzyme complex was produced which included beta (l-*3) glucanase and protease. Optimum activity of these two enzymes was achieved at a dilution rate of 0.05 h" 1 . The potential of continuous-flow enrichment culture for the selection of microorganisms producing extra cellu¬ lar enzymes has been little realized. Continuous cul¬ ture has a big advantage over batch culture in relation to enzyme production. In continuous culture studies it has been possible to increase the concentration of the lytic enzymes by more than one order of magnitude com¬ pared to the batch production. It is also possible to regulate the ratio of glucanase to protease in the lytic enzyme system by using different inducers or altering the dilution rate. This study has shown that in continuous culture it is possible to produce enzyme systems with desired charac¬ teristics for a particular application (e.g. for wall degradation or to isolate a particular product from inside the cell) . Summary of the Invention • The present invention is a method for preparing a yeast cell lytic enzyme system having desired beta (l-*3) glucanase and protease activities. A suitable bacteri¬ um which produces the lytic enzyme system is inoculated onto an appropriate growth medium containing predeter¬ mined amounts of a sugar as the carbon source (for example, sugar) and an inducer of lytic enzyme activi¬ ty. The bacterium is continuously fermented aerobical¬ ly at an appropriate dilution rate, the dilution rate being varied to obtain the desired beta (l-»3) glucanase and protease activities. The resulting lytic enzyme system is recovered. The bacterium may be one or more of the group consist¬ ing of Cytophaga, Qers QVi-a or Arthrobacter. n flf! H r,lfln of the Figures Fig. 1 Cell and Enzyme Concentrations in Cvtophaga NCIB 9497 Continuous Culture as a function of dilution rate (h "1 ) . The medium is comprised of 5 g/L glucose 5 and 10 g/L yeast extract. Values are for beta (1→3) glucanase (B(l-*3) , U/L, (A)); reducing sugars (R.S. , g/L, (•)); protease (P, u, (Q) (u=l% hydrolysis in 20 min.); yeast lytic activity (YLA, U, ( Δ.) ) (U = % de¬ crease in OD 6 7o after 15 min.); Cells (Cells, OD Q-J Q ' 10 (0) ) . Fig. 2 Specific Enzyme Activity in Continuous Cul¬ ture of Cytophaga sp. (activity/g cells) as a function of dilution rate (h "1 ) . The medium is comprised of 5 £5 g/L glucose and 10 g/L yeast extract. Values are for yeast lytic activity (YLA, % decrease in OVQ-J Q after 15 min./g cells, (A)); protease (P, u/g cells, (D)); beta (1→3) glucanase (B(l-*3) , U/L/g cells, ( )). 20 Fig.3. Specific Rate of Enzyme Synthesis in Continu¬ ous Culture of Cytophaga sp. (activity/g cells h) . The medium is comprised of 5 g/L glucose and 10 g/L yeast extract. Values are for beta (1→3) glucanase (B(l→3) , U/L/g cells h, (A)); protease (P, u/g cells h, ( □) ) ; 25 yeast lytic activity (YLA, % decrease in OD/g cells h, (Δ)). Fig. 4 Productivity in Continuous Culture of Cytophaga sp. (activity/L h) . The medium is comprised 30) of 5 g/L glucose and 10 g/L yeast extract. Values are for yeast lytic activity (YLA, % decrease in OD/L h, (Δ)); protease (P, u/L h, (Q)); beta (1+3) glucanase (B(l->3), U/L/L h, (A)); Cells (Cells, OD 67Q /L h, (0)). 35 Fig. 5 Cell and Enzyme Concentrations in Oerskovia xanthineolytica Continuous Culture as a function of dilution rate (h" 1 ) . The medium is comprised of 2 g/L glucose and 2 g/L glucan. Values are for beta (143) glucanase (B(l+3), U/L, (A)); protease (P, u, ( Q) ) ; reducing sugars (R.S. , g/L, (#)); yeast lytic activity (YLA, ϋ, (Δ)) (ϋ = % decrease in OD 670 in 15 min.); Cells (Cells, (*/mL) x 10 9 , (O)) mannanase (M,U/L, Fig. 6 Cell and Enzyme Concetration in Oergkovia xanthineolytica Continuous Culture as a function of dilution rate (h "1 ) . The medium is comprised of 8 g/L glucose and 0.5 g/L glucan. Values are for beta (1+3) glucanase (B(l→3) , U/L, ( A)); protease (P, u (Q)); glucose (G, g/L, (#)); yeast lytic activity (YLA, U, (Δ)) (ϋ = % decrease in OD 670 i n 15 min.); Cells (Cells, (#/mL) x 10 9 , (O)). Fig. 7 Beta (1-3) Glucanase and Protease Activities in Continuous Culture of Oerskovia sp. as a function of dilution rate (h -1 ) . The medium is comprised of 8 g/L glucose and 0.5 g/L glucan or 2 g/L glucose and 2 g/L glucan. Values are for beta (1→3) glucanase (B(l-*3) , U/L, (A)); protease (P,. u, (D)). Fig. 8 Specific Enzyme Activity in Continuous Cul¬ ture of Oerskovia sp. (activity/g cells) as a function of dilution rate (h _1 ) . The medium is comprised of 2 g/L glucose and 2 g/L glucan. Values are for beta (l→ 3) glucanase (B(l-73) , U/L/g cells, (A)); protease (P, u/g cells, (£])) mannanase (M, U/L/g cells, (O)); yeast lytic activity (YLA, % decrease in OD/g cells, ( Δ>>. Fig. 9 Specific Enzyme Activity in Continuous Cul¬ ture of Oerskovia sp. (activity/g cells) as a function of dilution rate (h" 1 ). The medium is comprised of 8 g/L glucose and 0.5 g/L glucan. Values are for beta (l-a-3) glucanase (B(l->3) , ϋ/L/g cells, ( ))? protease (P, u/g cells, (Q)); yeast lytic activity (YLA, % decrease in OD/g cells, (Δ)). Fig. 10. Specific Rate of Enzyme Synthesis in Continu¬ ous Culture of Oerskovia sp. (activity/g cells h) as a function of dilution rate (if 1 ) . The medium is com¬ LU prised of 2 g/L glucose and 2 g/L glucan. Values are for protease (P, u/g cells h, (Q)); mannanase (M, U/L/g cells h, (Q)); beta (1→3) glucanase (B(l->3) , U/L/g cells h, (A)); yeast lytic activity (YLA, % decrease in OD/g cells h, (Δ)). 5 Fig. 11 Specific Rate of Enzyme Synthesis in Continu¬ ous Culture of Oerskovia sp. (activity/g cells h) as a function of dilution rate (h "1 ) . The medium is com¬ prised of 8 g/L glucose and 0.5 g/L glucan. Values are (r for protease (P, u/g cells h, (CI) ) ; beta (l-»3) glucanase (B(l-i>3), U/L/g cells h, (A)); yeast lytic activity (YLA, % decrease 'in OD/g cells h, (Δ))« Fig. 12 Productivity in Continuous Culture of 5 Oerskovia sp. as function of dilution rate (if 1 ) . The medium used was comprised of 2 g/L glucose and 2 g/L glucan. Values are for yeast lytic activity (YLA, % decrease in OD/L h, ( Δ) ) ; beta (1→3) glucanase (B(l-» 3), U/L/L h, (A))? protease (P, u/L h, (Q)); manna- nase (M, U/L/L h, (O)); Cells (Cells, (#/mL) x 10 9 , (O). 5 Fig. 13 Productivity in Continuous Culture of Oerskovia sp. as a function of dilution rate (if 1 ) . The medium used was comprised of 8 g/L glucose and 0.5 g/L glucan. Values are for yeast lytic activity (YLA, % decrease in OD/L h, (Δ)) * beta (l-*3) glucanase (B(l-? 3), ϋ/L/L h, (A)); protease (P, u/L h, (CD); dry weight (D.W., g/L/L h (0)). 1-gtaiTed Description of the Invention The present invention is a method for preparing a yeast cell lytic enzyme system having desired beta (l-»3) glucanase and protease activities. A suitable bacteri- 5 urn which produces the lytic enzyme system is inoculated onto an appropriate growth medium containing predeter¬ mined amounts of carbon source and an inducer of lytic enzyme activity. The bacterium is continuously fer¬ mented aerobically at an appropriate dilution rate, the • Ltt i dilution rate being varied to obtain the desired protease and beta (1→3) glucanase activities. The resulting lytic enzyme system is recovered. The bacterium may be one or more of the group consist- 53 ing 0 f cytophaga. Qers ovia or Arthrobacter. The method may consist of inoculating Oerskovia onto a growth medium containing glucose as the carbon source and yeast wall glucan as the inducer. The growth medi- 0 *; um may contain up to 20 g/L of glucose and 20 g/L of yeast wall glucan. In particular, the growth medium may contain 8 g/L glucose and 0.5 g/L yeast wall glucan. The dilution rate for the continuous fermen¬ tation may be selected so it provides high beta (l-»3) 5 glucanase activity. In particular, the dilution rate may be between about 0.05 and about 0.20 "1 for high beta (1→3) glucanase activity. The dilution rate may also be selected so it provides high protease activity. In particular, the dilution rate may be between about 0 0.02 and about O.lOh "1 for high protease activity. The dilution rate may be selected so it provides high beta (1→3) glucanase activity and low protease activity. The dilution rate may be between about 0.15 and about O.20h _1 for high beta (1→3) glucanase activity and low 5 protease activity. Another growth medium for Oerskovia may contain 2 g/L glucose as the carbon source and 2 g/L yeast wall glucan as the inducer. The dilution rate for the con¬ tinuous fermentation may be selected so it provides 5 high beta (1+3) glucanase activity. In particular, the dilution rate may be between about 0.05 and about 0.14h _1 for high beta (1+3) glucanase activity. The dilution rate may also be selected so it provides high protease activity. In particular, the dilution rate ( may be between about 0.02 and about 0.14h _1 for high protease activity. The dilution rate may also be se¬ lected so it provides high beta (1*3) glucanase and low protease activity. In particular, the dilution rate may be between about 0.15 and about O^Oh *-1 for high 5 beta (1+3) glucanase activity and low protease activi¬ ty. The amount of inducer present may be an amount suffi¬ cient to produce high levels of beta (1+3) glucanase activity. Bacterial strains suitable for the method of this in¬ vention include wild type strains of Cytophaga f Oerskovia and Arthrobacter and derivatives thereof. The dilution rate which is suitable for the present invention may be between about 0.02 and about 0.40 if 1 . The continuous culture may be maintained at a pH and temperature suitable for preparing a yeast cell lytic enzyme system. Another aspect of the invention may consist of inocu¬ lating Cytophaga onto a growth medium containing glu- cose as a carbon source. In particular, the growth medium may contain 5 g/L glucose. The dilution rate for the continuous fermentation may be selected so it provides high beta (1+3) glucanase activity and high protease activity. The dilution rate may be between about 0.05 and about O.lOh" 1 for high beta (1+3) glucanase and high protease activity. The pH for this method may be about 7.0 and the temperature may be about 29°C Synthesis of enzymes, may be inducible, semi-constitu¬ tive or constitutive. Inducible enzymes are synthe¬ sized at a low level in the absence of inducers. The uninduced, basal level of enzyme synthesis can vary considerably. When the basal enzyme activity is high, it is classified as semi-constitutive. Constitutive enzymes are synthesized maximally in the presence or absence of an inducer. Several bacteria are suitable for the disclosed meth- od. One in particular, Cytophaga NCIB 9497, has been considered to be constitutive for yeast lytic enzyme synthesis. When Cytophaga NCIB 9497 is inoculated onto a medium of 10 g/L of yeast extract and 5 g/L of glucose, the specific .activities of the beta (1+3) glucanase and yeast lytic activity are high at dilution rates between 0.05 and O.lOh "-1 . In this range of dilu¬ tion rates the level of reducing sugars in the fermen¬ tation broth is low. Results indicate dual control of beta (1+3) glucanase synthesis by induction and catabolite repression. Between dilution rate of 0.03 and 0.07 if 1 catabolite repression is minimal because the low growth rate of the organism does not lead to an accumulation of repressing catabolites. Synthesis is regulated by the amount of inducer present. Growth rate increases with increasing dilution rate and as a result the rate of enzyme synthesis increases. At a dilution rate between 0.07 and 0.1 if 1 the concentra¬ tion of the repressor has reached a level high enough to cause significant catabolite repression. As the dilution rate increases the growth rate increases and catabolite repression becomes dominant over induction and the rate of enzyme production drops. - The regulation of protease enzyme synthesis does not appear to be under dual control by induction and cata¬ bolite repression in the range of dilution rates stud¬ ied (between 0.03 and 0.30h _1 ) . Protease synthesis is subject to catabolite repression but is not induced. Reducing sugars in the fermentation broth described above accumulated at dilution rates greater than 0.15 h . The reducing sugar content was 6.9 g/L, indicat¬ ing that most of the measured reducing sugars were glucose. At dilution rates up to 0.3 if 1 washout did not occur. The accumulation of reducing sugars at dilution rates above 0.15 h "1 indicates the presence of a second limiting substrate. This substrate is un¬ known. Dissolved oxygen was never limiting. Protease synthesis does not appear, from continuous culture studies, to be inducible. The activity levels therefore are similar in late batch culture and in continuous culture at low dilution rates. Enzyme lev¬ els in continuous culture at high dilution rates (when glucose accumulates) are similar to those in batch culture when approximately half the reducing sugars have been metabolized. It appears that the proteolytic activity is made up of activity from more than one protease enzyme and that the syntheses of these enzymes are not regulated to¬ gether. In carbon limited media, two peaks of spe¬ cific rate of enzyme synthesis exist; one at dilution rates above 0.15 h "1 and one at dilution rates below 0.15 h~ . The appreciable rate of enzyme synthesis at high dilution rates is evidence that not all the proteolytic enzymes are catabolite repressed. There is also evidence that one of the proteases may be induced by the second, unknown limiting substrate. The peak at low dilution rates indicates that one of the proteases may be weakly induced. Another suitable bacterium of the disclosed method is Oerskovia xanthineolytica. Continuous cultures were carried out using two different media; one with 2 g/L of glucose and 2 g/L of glucan and the other with 8 g/L of glucose and 0.5 g/L of glucan. In both continuous cultures enzyme activities were high at low dilution rates (below 0.15 if 1 ) . The beta (1+3) glucanase activity on the medium with 8 g/L glucose and 0.5 g/L of glucan is higher than that produced on the medium with 2 g/L glucose and 2 g/L glucan. The same is true of protease activity. There is a distinction between the beta (1+3) glucanase specific activities in the two continuous cultures. In the medium with 2 g/L glucose and glucan there is a sharp peak of beta (1+3) glucanase specific activity at low dilution rates. The maximum specific activity is more than three times that on the medium of 8 g/L glu¬ cose and 0.5 g/L of glucan. Beta (1+3) glucanase spe¬ cific activity in the medium containing 2 g/L glucose and glucan appears to be controlled by both induction and catabolite repression. Protease does not appear to be induced at low dilution rates, but is subject to catabolite repression. Materials and Methods Cytophaga sp. NCIB 9497 was obtained f rom the National Collection of Industrial Bacteria. (Aberdeen, Scotland) . QersKovia xanthineolytica LL-G109 was a gift f rom M. Lechavalier, Rutgers University, New Jersey, USA. ArthrgbaςtQr sp. GJM-1 was obtained f rom C. Ballou, University of California, Berkeley, USA. Saccharomyce^ cerevisiae NCYC 1006 was f rom the National Collection of Yeast Cultures, Norwich, UK. Saccharomyces £aιls__. berσensis was a gift f rom the Stroh Brewing Company, Michigan, USA and the bakers yeast used was Red Star active dried yeast f rom the Universal Food Corporation, Wisconsin, USA. All chemicals used were Analar grade except those list¬ ed below. Yeast extract - "Ardamine Yep", (autolysed yeast ex- tract powder), was supplied by Yeast Products Inc., New Jersey, USA. Glucose (used in fermentation media) - technical grade, Sigma Chemical Company, Missouri, USA. Nutrient Agar, Maltose and Peptone technical grade - Difco Laboratories, Michigan, USA. Antifoam - a 30% aqueous solution of a 100% active silicone polymer, Sigma Chemical Company, Missouri, USA. Glucan, prepared by alkali extraction from bakers yeast, (Manners e_fc ϋl. , 1973a) was a gift from J. Hunt¬ er, Department of Chemical Engineering and Applied Chemistry, Columbia University, New York, USA. It was sieved and the fraction smaller than 177 microns (mesh #80) was used. Yeast cell walls (used as an inducer) were prepared from Saccharomyces carlsberσensis disrupted in a Dyno mill (Willy A. Bachofen AG, Switzerland) for 20 minutes (aproximately 90% disruption) , washed with distilled water and filtered (Whatman #2 paper). For the growth of inocula and for some batch experi¬ ments Erlenmeyer flasks were used. Cultures were incu¬ bated in an incubator-shaker (Model G 26) , New Brunswick Scientific Co. , Inc. , New Jersey, USA. In fermentations with Cytophaga sp. a lyophilised culture was used for each inoculum. Inocula (10% v/v) were grown for 12-17 hours. Bioflo C 30 and C 32 fer enters (New Brunswick Sci. Co. Inc.) were used for both batch and continuous culture studies. The C 32 vessel has a volume of 2 L (1.2 L working volume) and the C 30 a volume of 750 mL (350 mL working volume) . These fer¬ menters were fitted with automatic temperature and pH control and a dissolved oxygen (DO) probe and meter. Media For Cytophaga sp. : 5.0 g/L glucose 10.0 g/L yeast extract For Oerskovia sp. and Arthrobacter sp. 2.0/8.0 g/L glucose 2.0/0.5 g/L glucan 0.5 g/L K 2 HP0 4 0.3 g/L NaH 2 P0 4 .2H 2 0 5.0 g/L NH 4 C1 50 mL Trace element mix pH 6.8 Trace element mix: 0.250 g/L MgS0 4 .7H 2 0 0.050 g/L CaCl 2 0.020 g/L ZnS0 4 .7H 2 0 0.020 g/L MnS0 4 .4H 2 0 0.005 g/L CuS0 4 .5H 2 0 0.100 g/L FeS0 4 .7H 2 0 0.600 g/L EDTA Na 2 H 2 0 ASSAYS Cell concentration was estimated in three ways: opti¬ cal density (OD) , dry weight (DW) , or viable cell count (colony count) . Optical Density Optical Density was measured in a Spectronic 21 spec- trophotometer (Bausch and Lomb, New York, USA) . Sam¬ ples were diluted before reading to fall within the range from 0 to 0.6 on the absorbance scale. When used to estimate growth optical densities were read at 670 nm. Dry Weight 5; A known volume of culture was filtered through a previ¬ ously dried and weighed "Metricel" membrane fiter (0.45 microns), Gelman Sciences Inc., Michigan, USA. The filter was then dried to constant weight at 80 C. Dry 0" weight (DW) was calculated and expressed in grams of cells per litre of culture broth. Colony Count The colony count method was used to estimate growth in fermentations containing insoluble substances where optical density and dry weight were not useful. Serial dilutions of the culture borth were made in sterile distilled water. O.lmL of the appropriate dilutions - were plated in duplicate. After 72 hours the colonies were counted and the number of cells per unit volume calculated. Continuous fermentations were carried out in Bioflo C _ 30 or C 32 fermenters. 3 volume changes were allowed before steady state samples were taken and 3 samples were taken at 1 hour intervals at each point. The fraction of the original material remaining in the chemostat after 3 volume changes is 0.05 (Pirt, 1975). 0 When using the 350mL (C 30) fermenter the smallest possible samples (less than 5 mL) were taken to avoid altering the fermenter volume and thus the steady state conditions more than necessary. 5 Sterile antifoam was added aseptically to the medium resevoir after sterilisation at a concentration of 0.25 mL/L of a 30% aqueous solution per litre of medium. If added before autoclaving clumps formed on the surface of the medium and the effect of the antifoam was lost, 5. the performance of the DO probe was also affected. When insoluble inducers were used they were added di¬ rectly to the medium resevoir which was stirred throughout the fermentation. The tubing (silicone) was 10." checked daily for buildups of insoluble material. Culture purity was checked daily by plating two 0.1 L sampels of culture borth on nutrient agar plates. 15; Immediately after removal from the fermenter the sample to be used for enzyme assays was filtered (membrane filter, 0.45 microns) and frozen. When larger volumes of enzyme were needed the supernatent was centrifuged at 2000 rpm for 15 minutes, separated and the enzyme 20 ' preparation frozen. Yeast Lytic Activity The method used to estimate the overall lytic activity 5 was decrease in optical density in an incubation of whole yeast cells, lytic enzyme and buffer. Decrease in optical density: equal volumes of enzyme preparation, yeast substrate (a 1/400 w/v solution of 3 Q washed, packed cells) and buffer (50 mM Tris-HCl, pH 7.3) were mixed in a spectrophotometer tube which was then incubated at 37 C. Periodically the tube was removed from the water bath, mixed and the optical density at 670 nm read. Yeast autolysis was followed 5 by incubating 1 volume of yeast with 2 volumes of buff¬ er. Yeast lytic activity is expressed in units (U) where 1U equals a 1% decrease in OD after 15 min. in the range of 20% to 50% decrease. Glucanase and Mannanase Activities Beta (1+3) Glucanase activity assay: equal volumes of enzyme, laminarin (a 3% w/v solution) and buffer (50 mM Tris-HCl, pH 7.3) were incubated at 37 C. The reaction lα was terminated by boiling in a water bath for 5 min¬ utes. Reducing sugars released were assayed using the Nelson-Somogyi method (Nelson, 1944) or .the Micro Nelson method (Spiro, 1966) . Standard curves were prepared using glucose. 1 5 Mannanase activity was assayed in the same way Beta (1+3) glucanase except that the substrate used was a 0.5% solution of mannan. Glucanase and mannanase activities are expressed in 20 international units, 1 U is that amount of enzyme which releases 1 umole of glucose per minute under specified conditions. Proteolytic Activity 25 Protease activity was measured by the method of Rowley and Bull (1977) . The substrate used was azocasein at a concentration of 2.5 g/L. Equal volumes of substrate and enzyme were incubated at 37 C for 20 minutes. The 30 reaction was terminated by the addition of 2 mL of 3 M TCA (trichloroacetic acid) . After centrifugation at 2000 rpm for 30 minutes the absorbance of the superna¬ tant was read at 400 n . Various blanks and controls 35 were run. The activity is expressed in units (u) where lu equals 1% hydrolysis in 20 min. in the range from 0% to 30%. A unit corresponds to the solubilization of 0.00125 mg. protein per min. per ml. of enzyme solu¬ tion. Glucose Assay Glucose concentrations were determined by the PGO (Per- oxidase Glucose Oxidase) method, Sigma Technical Bulle- tin No. 510. Example I Cytophaga NCIB 9497 was grown in continuous culture. The medium contained 10 g/L of yeast extract and 5 g/L of glucose. The pH was controlled at 7 and the temper¬ ature at 29°C. Steady state conditions at dilution rates from 0.03 h "1 to 0.30 h "1 were analyzed for cell concentration, beta (1+3) glucanase, protease, mannanase and yeast lytic activities as well as reduc¬ ing sugars present in the fermentation broth. The level of glucose (reducing sugars) in the fermenta¬ tion broth was between 0.5 and 0.8 g/L up to a dilution rate of 0.15 if 1 . At dilution rates above 0.15 h -1 glucose accumulated and another substrate became limit¬ ing. At dilution rates above 0.15 if 1 the synthesis of beta (1+3) glucanase is repressed by glucose. Yeast lytic activity is mainly attributable to production of proteolytic enzymes. Activities of beta (1+3) glucanase, protease, mannanase and overall yeast lytic activity are similar to those obtained in batch cul- ture. The beta (1+3) glucanase and protease activities are highest at a dilution rate of about 0.07 h "1 where there is a corresponding peak in yeast lytic activity. The enzyme system has a high beta (1+3) glucanase/protease ratio. Specific activity (activity/g cells) is calculated using a dry weight per unit optical density correlation of 0.93 g per liter per unit optical density. For this fermentation, beta (1+3) glucanase activity exhibits a peak of specific activity at dilution rates between about 0.05 and about 0.07 h" 1 . At dilution rates above and below this range the specific activities drop sig¬ nificantly. At dilution rates below 0.07 h~ catabolite repression is minimal and the rate of glucanase synthesis is dependent mainly upon the con¬ centration of inducer present. Catabolite repression increases with increasing dilution rate until it be¬ comes dominant over induction at dilution rates of about 0.07 h" 1 and above. Cytophaga NCIB 9497 has in the past been classified as constitutive for enzyme synthesis. It appears from these continuous culture studies that enzyme synthesis in Cytophaga NCIB 9497 is regulated by induction and catabolite repression. The specific activity profile for the proteolytic en¬ zyme shows a steady decline with no peak. It does not appear to be inducible but is subject to catabolite repression. The specific rate of enzyme synthesis (also called the "specific productivity") is the amount of enzyme activ¬ ity produced per gram of cells per hour. In the range specific rates of beta (1+3) glucanase and protease synthesis both exhibit peaks. At dilution rates above 0.15 if 1 the rate of glucanase synthesis is low but the rate of protease synthesis shows another peak. Productivity is activity per liter per hour for enzyme measurement and optical density per liter per hour for measurement of biomass growth. At dilution rates above 0.25 h "1 a peak of high productivity but low concentra¬ tion occurs with proteolytic and yeast lytic activi- ties. Productivity of beta (1*3) glucanase activity is low at this range of dilution rates. The productivity of biomass increases slowly with increasing dilution rate. Between rates of about 0.03 and about 0.15 if 1 , all enzyme activities exhibit a sharp peak in produc- tivity. Productivity of beta (1+3) glucanase activity was 20 times greater and yeast lytic activity 4 times greater than such productivity in batch culture. Example II Qegsfrgyja xanthinedytica T.L-G109 was grown in continu¬ ous culture. The medium contained 2 g/L glucose as the carbon source and 2 g/L yeast wall glucan as the induc- er. Enzyme concentrtion and growth are monitored as well as glucose present in the fermentation broth over a range of dilution rates from 0.03 to 0.38h -1 . The level of glucose in the fermentation broth was about 0.02 g/L throughout the range of dilution rates used. The level of beta (1*3) glucanase activity is low when dilution rates are below 0.05h _1 . The level increases with increasing dilution rate so that activity is high at dilution rates between about 0.05 and about 0.14b "1 . Dilution rates above 0.14h~ 1 result in low activity. Protease activity is low throughout the range of dilu- tion rates studies, and very low at dilution rates above 0.15h _1 . Specific activity (activity/g cells) is calculated using a dry weight per unit optical density correlation ; of 0.61 g per liter per unit optical density. For this fermentation, the specific activity of beta (1*3) glucanase is high at dilution rates between about 0.03 and about O.OΘh "1 , with a peak at a dilution rate of about 0.05h~ . Specific activities at dilution rates below 0.03h _1 and above 0.09h _1 are low. Protease specific activity is greatest at dilution rates below Q.05h~ . Increasing dilution rates result in low protease specific activity. . The specific rate of enzyme synthesis (specific produc¬ tivity) is the amount of enzyme activity produced per gram of cells per hour. For beta (1+3) glucanase, this value is greatest at dilution rates below O.lSh "1 . At dilution rates above O.lSh "1 the specific rate of en- zyme synthesis is low. For protease, this value is highest at low dilution rates but diminishes to a low synthesis rate at dilution rates above O.lOh -1 . Productivity is activity per liter per hour for enzyme measurement, and optical density per liter per hour for measurement of biomass growth. Beta (1*3) glucanase activity exhibits high productivity at low dilution rates (below 0.2h _1 ) with a maximum at about O.lSh" 1 . Protease productivity is maximized at a dilution rate of about 0.15" 1 as well. Protease productivity above dilution rate of 0.15h -1 is lower but constant, and below a dilution rate of O.lSh "1 steadily declines. Example III Oerskovia xanthineolytica LL-G109 was grown in continu¬ ous culture. The medium contained 8 g/L glucose as the carbon source and 0.5 g/L yeast wall glucan as the inducer. Enzyme concentration and growth are monitored as well as glucose present in the fermentation both over a range of diltuion rates for 0.03 to 0.38I1 "1 . The glucose level was close to 0 g/L up to a dilution rate of O^δif 1 , above which it accumulates. The level of beta (1+3) glucanase activity is high at dilution rates between about 0.03 and about 0.2h -1 . Activity is low at dilution rates above 0.2b" 1 . Cell number increased at low dilution rates, dropping drastically above O.lSh "1 and below O.lh "1 . Protease activity is low throughout the range of dilu¬ tion rates studies, and very low at dilution rates above O.lSh "1 . Specific activity (activity/g cells) is calculated using a dry weight per unit optical density correlation of 0.61 g per liter per unit optical density. For this fermentation, the specific activity of beta (1+3) glucanase is greatest at low dilution rates (below O.lSh "1 ). For protease this value is highest at dilu¬ tion rates above 0.25h _1 . Productivity is activity per liter per hour for enzyume measurement, and optical density per liter per hour for measurement of biomass growth. Beta (1*3) glucanase activity exhibits high productivity at diltuion rates below 0.2h _1 , with a maximum at about O.lSh" 1 . Protease productivity above a dilution rate of O.lSh" 1 is lower but constant, and below a dilution rate of O.lSh "1 steadily declines. -

Claims: What is Claimed is: 1. A method for preparing a yeast cell lytic enzyme system having desired beta (1*3) glucanase and protease activities which comprises: 5 a. inoculating a suitable bacterium which pro¬ duces the lytic enzyme system onto an appropriate growth medium containing predetermined amounts of a carbon source and an inducer of lytic enzyme j 0 activity; b. continuously fermenting the bacterium aerobi¬ cally at an appropriate dilution rate, the dilu¬ tion rate being varied to obtain the desired ,- protease and beta (1+3) glucanase activities; and c. recovering the resulting lytic enzyme system. 2. A method of claim 1, wherein the bacterium is 20 Cytophag , Oerskovia or Artfrrobacter. 3. A method of claim 2, wherein the bacterium is Qerskgvia. 4. A method of claim 1, wherein the carbon source- is 25 glucose. 5. A method of claim 4, wherein the amount of glucose is up to about 20 g/L. 30 6. A method of claim 1, wherein the inducer is yeast wall glucan. 35 7. A method of claim 6, wherein the amount of yeast wall glucan used as the inducer is up to about 20 g/L. 8. A method of claim 1, wherein the growth medium is comprised of about .8 g/L glucose and about 0.5 g/L yeast wall glucan. 55 9. A method of claim 1, wherein the dilution rate provides high beta (1*3) glucanase activity. 10. A method of claim 9, wherein the dilution rate is HE between about 0.05 and about O.lOh -1 . 11. A method of claim 1, wherein the dilution rate provides high protease activity. i s: 12. A method of claim 11, wherein the dilution rate is between about 0.02 and about O.lOh "1 . 13. A method of claim 1, wherein the dilution rate maintained provides high beta (1*3) glucanase activity 20 and low protease activity. 14. A method of claim 13," wherein the dilution rate is between about 0.15 and about 0.20b "1 . 255 15. A method of claim 1, wherein the growth medium is comprised of about 2 g/L glucose and about 2 g/L yeast wall glucan. 16. A method of claim 1, wherein the dilution rate 30 maintained provides high beta (1+3) glucanase activity. 17. A method of claim 16, wherein the dilution rate is between about 0.05 and about 0.14h _1 . 5 18. A method of claim 1, wherein the dilution rate provides high protease activity. 19. A method of claim 18, wherein the dilution rate is between about 0.02 and about 0.14h~ 1 . 20. A method of claim 1, wherein the dilution rate maintained provides high beta (1*3) glucanase activity and low protease activity. 10. 21. A method of claim 20, wherein the dilution rate is between about 0.15 and about 0.20h _1 . 22. A method of claim 2, wherein the bacterium is Cytophaga. 15 23. A method of claim 22, wherein the carbon source comprises glucose and yeast extract. 24. A method of claim 23, wherein the amount of glu¬ 20 cose used is up to about 20 g/L. 25. A method of claim 23, wherein the amount of yeast extract used is up to about 20 g/L. Δ 26. A method of claim 22, wherein the growth medium is comprised of about 5 g/L glucose and about 10 g/L yeast extract. 27. A method of claim 22, wherein the growth medium pH 30- is about 7.0. 28. A method of claim 22, wherein the growth medium temperature is about 29°C. 35 29. A method of claim 22, wherein the dilution rate maintained provides high beta (1*3) glucanase activity and high protease activity. 5 30. A method of claim 29, wherein the dilution rate is between about 0.05 and about O.lOh" 1 . 31. A yeast cell lytic enzyme system produced by any of the methods of claims 1, 2, 3, or 22. 5 0 * 5 0 5

Inventors: ANDREWS BARBARA A, ASENJO JUAN A, ANDREWS, BARBARA, A., ASENJO, JUAN, A.
Applicants: UNIV COLUMBIA, THE TRUSTEES OF COLUMBIA UNIVERSITY IN THE CITY OF
Application year: 1986
Main classification: C12N9
IPC codes: C12N9, C12R1