CN1035131A - 多糖的生产方法 - Google Patents
多糖的生产方法 Download PDFInfo
- Publication number
- CN1035131A CN1035131A CN88109243A CN88109243A CN1035131A CN 1035131 A CN1035131 A CN 1035131A CN 88109243 A CN88109243 A CN 88109243A CN 88109243 A CN88109243 A CN 88109243A CN 1035131 A CN1035131 A CN 1035131A
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- Prior art keywords
- starch
- class
- fermentation
- polysaccharide
- saccharifying enzyme
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Classifications
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
- C12P19/00—Preparation of compounds containing saccharide radicals
- C12P19/04—Polysaccharides, i.e. compounds containing more than five saccharide radicals attached to each other by glycosidic bonds
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12N—MICROORGANISMS OR ENZYMES; COMPOSITIONS THEREOF; PROPAGATING, PRESERVING, OR MAINTAINING MICROORGANISMS; MUTATION OR GENETIC ENGINEERING; CULTURE MEDIA
- C12N1/00—Microorganisms, e.g. protozoa; Compositions thereof; Processes of propagating, maintaining or preserving microorganisms or compositions thereof; Processes of preparing or isolating a composition containing a microorganism; Culture media therefor
- C12N1/38—Chemical stimulation of growth or activity by addition of chemical compounds which are not essential growth factors; Stimulation of growth by removal of a chemical compound
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
- C12P19/00—Preparation of compounds containing saccharide radicals
- C12P19/04—Polysaccharides, i.e. compounds containing more than five saccharide radicals attached to each other by glycosidic bonds
- C12P19/06—Xanthan, i.e. Xanthomonas-type heteropolysaccharides
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
- Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10S435/00—Chemistry: molecular biology and microbiology
- Y10S435/8215—Microorganisms
- Y10S435/822—Microorganisms using bacteria or actinomycetales
- Y10S435/91—Xanthomonas
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Life Sciences & Earth Sciences (AREA)
- Wood Science & Technology (AREA)
- Zoology (AREA)
- Health & Medical Sciences (AREA)
- Biotechnology (AREA)
- Genetics & Genomics (AREA)
- Bioinformatics & Cheminformatics (AREA)
- Microbiology (AREA)
- Biochemistry (AREA)
- General Chemical & Material Sciences (AREA)
- General Engineering & Computer Science (AREA)
- General Health & Medical Sciences (AREA)
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Abstract
本发明涉及一种利用微生物使碳水化合物发酵
来制取生物聚合物的方法。
该方法是在糖化酶存在下,在含有作为可同化碳
源的淀粉的含水营养介质中进行发酵。
特别应用于呫吨胶的生产。
Description
本发明涉及用微生物对碳水化合物进行发酵以生产多糖的一种改进方法。更准确地说,本发明涉及利用淀粉或淀粉水解产物作为营养碳源的一种发酵方法。
高分子量的发酵多糖或生物聚合物,由于其在含水介质中的增稠性、粘性和稳定性,以不断增长的方式在许多工业中得到应用。另外,由于呫吨胶的特殊流体性能,它在建筑、油漆、造纸、纺织品、化妆品、食品、农业、水处理、钻探、石油回收及其他等各个领域中都得到应用。
生物聚合物是在含水营养介质中经微生物需氧培养制得的。
呫吨胶由黄单胞菌属制得,相同类型的生物聚合物可以由微生物的许多品种产生,其中包括土壤杆菌属、节菌属、产碱杆菌属(琥珀酸聚糖)、假单胞菌属(左聚糖)、根瘤菌属、小菌核属(硬葡聚糖)。这些多糖是高分子量的,一般超过1×106,并且是由葡萄糖、甘露糖、半乳糖、鼠李糖、葡糖醛酸、甘露糖醛酸、guluronique酸与醋酸盐和丙酮酸盐的衍生物结合组成的。它们特定的结构与它们的性质在Industrial Gums-Whistler-第二版,(1973)中的第21-23章以实例作了描述。
有关生产发酵多糖的出版物有许多。如在US-A-3020206、3251749、3391060、3271267、3427226、3433708、3455786、3485719、3594280、4154654、4282321中描述了生产呫吨胶的方法。
含水的营养介质,除不同的生长元素外,一般都含有可同化的碳水化合物作碳源。合适的碳水化合物包括葡萄糖、蔗糖、果糖、麦芽糖、乳糖、可溶性淀粉及其水解产物。尽管把未加工的淀粉描述为合适的碳源,但对于象葡萄糖之类的单糖来说大大延长发酵周期应该是非常不利的。而且,微生物不能消耗所有还原性糖。发酵结束时残余糖的存在,在分离多糖之前,一方面能对使糖汁降解的污染源的发展提供有利的介质,另一方面,当进行巴斯德灭菌法热处理和可能的澄清时,有使产品着色的危险。
本发明的主要目的在于提出一种经济的发酵方法,该方法利用淀粉作碳源,并其产率至少与用葡萄糖、或含葡萄糖较多的淀粉水解产物作碳源所得到的产率相等。
已发现,借助于淀粉进行酶水解的同时产生的微生物进行发酵,可以以经济的方式生产多糖产物。这种方法允许以一种意外的方式得到多糖,对于由未加工的淀粉所制得的多糖来说,该多糖则具有改变的流体性质。另外的优点是减少发酵的时间,除去了低分子量的残余糊精,而且改善了产率。在含有作为可同化碳源的淀粉和含水营养介质中用微生物的需氧发酵生产本发明多糖的方法,其特征在于在至少一种糖化淀粉分解酶的存在下进行补充发酵。
本发明中用作碳源的淀粉可以是任何谷物淀粉,如小麦、玉米、高粱、稻、木薯粉、黑麦、燕麦的淀粉,或象土豆淀粉的块茎淀粉。
“淀粉”一词按本说明书描述应包括呈水悬浮液的未加工的淀粉和淀粉不完全水解生成的淀粉水解产物,如同流体化淀粉、淀粉糖浆以及富右旋糖的水解产物。淀粉的水解产物用它们的水解度彼此区分开来,而水解度用右旋糖当量D.E.、含有的低聚糖和较高的多糖表示。流体化淀粉的D.E.约在3至20之间,并一般限制多糖为50至95%,聚合度超过G7(7个葡萄糖单元)。低右旋糖当量的淀粉糖浆或葡萄糖浆的D.E.在约20至68之间,超过G7的多糖为10至50%。淀粉水解产物或富右旋糖糖浆的D.E.能达到90-98%。这类淀粉水解产物的制备技术已是众所周知。习惯上,用酸解和/或借助一种α液化淀粉酶酶解,再可能用一种β淀粉酶酶解制得流体化淀粉和淀粉糖浆。对于富葡萄糖的水解产物,最经常地用一种分为两个步骤的方法转化淀粉,即α液化淀粉酶的作用,然后一种糖化酶的作用,即葡糖淀粉酶,同样它也以淀粉葡糖苷酶为人所知。
在实施本发明方法时,人们最好利用淀粉糖浆,而更好的是流体化淀粉。从经济的观点来看,利用富葡萄糖水解产物不是有利的,因为这是一个很长的予糖化阶段,即乖谖露瘸?0℃和PH4.5-5时淀粉葡糖苷酶的最大活性条件下也是如此。
在消毒后,按照本发明的方法以未纯化的形式可以直接使用淀粉及其水解产物。人们当然可以使用象麦芽糊精这样经纯化、浓缩或脱水的工业产品。
为了满足在发酵介质中含有1至15%(重量)的葡萄糖,在发酵介质中有必需量的淀粉。
以干基的未加工淀粉表示,其合适量是在5-200克/升之间,最好是在10-150克/升(发酵介质中)。
在含有一种由高分子量多糖产生的微生物的发酵介质中,按照本发明方法添加的糖化淀粉酶是能将淀粉的右旋糖转换成葡萄糖和麦芽糖。作为糖化酶人们可列出α糖化淀粉酶,如Bacillus subtilis var.amylosaccharitiens α淀粉酶、α真菌淀粉酶、β淀粉酶、葡糖淀粉酶、异淀粉酶、支链淀粉酶,这些酶可以单独使用或混合使用。
由于葡糖淀粉酶的优良特性,人们优先使用它。葡糖淀粉酶可以是诸如归属于曲霉属、内孢霉属或根霉属类的所有真菌葡糖淀粉酶。尤其是在利用未加工淀粉作碳源的情况下,除了糖化酶外,还能利用液化酶,例如α液化淀粉酶-β淀粉酶的混合物或α-液化淀粉酶-葡糖淀粉酶的混合物。工业上酶的制备方法在l′ouvrage Encycl.of pol.sc.Vol 6,Pp 46-53中作了描述。
为了进行淀粉的糖化,各自的液化,在发酵介质中加入必需量的糖化的、可能液化的淀粉酶。所使用的最小量是介质中酶的活性,淀粉量和D.E.的函数,并且很容易由技术人员确定。就一般方法而言,对每克淀粉(以干料表示)加入0.02至4酶活度单位,最好加入0.1至2酶活度单位的量就足够了。一种由NOVO INDUSTRY投入商品生产的其名称是1′AMG 200L 的糖化酶是一种葡糖淀粉酶。按发酵介质中液化淀粉中所含固体重量为基,上述酶的加入量为0.01至2%(重量),最好为0.05至1%(重量)。
本发明的借助微生物使糖类发酵的方法是可以应用于制备所有外细胞多糖。诸如细菌、酵母、 、海藻许多微生物都能生产外细胞多糖。可引用如下的微生物:
-归属于黄单胞菌属类的细菌,更准确地说归属于Bergey′s manual of deferminative bacteriology(第八版-1974-Williams N.Wilkins C0Baltimore)叙述的种类,如秋海棠黄杆菌(Xanthomonas begoniae)、
甘兰里腐病黄杆菌(Xanthomonas Campestris)、
胡萝葡叶斑病黄杆菌(Xanthomonas Carotae)、
常春藤叶斑病黄杆菌(Xanthomonas hederae)、
紫罗兰白霉病黄杆菌(Xanthomonas incanae)、
棉角斑病黄杆菌(Xanthomonas malvacearum)、
罂粟黑斑病黄杆菌(Xanthomonas papavericola)、
菜豆疫病黄杆菌(Xanthomonas phaseoli)、
Pisi黄杆菌(Xanthomonas pisi)、
甘蔗流胶病黄杆菌(Xanthomonas vasculorum)、
辣椒斑点病黄杆菌(Xanthomonas vesicatoria)、
莴苣褐斑病黄杆菌(Xanthomonas vitians)、
天竺葵叶斑病黄杆菌(Xanthomonas pelargonii);
归属于节细菌属类的细菌,更准确地说归属于Arthrobacter stabilis、Arthrobacter viscosus;归属于欧文氏菌属类;归属于固氮菌属类,更准确地说归属于印度固氮菌(Azotobacter indicus);归属于土壤杆菌属,更准确地说归属于放射形土壤杆菌,根病土壤杆菌(Agrobacterium rhozigènes),根癌病土壤杆菌;归属于产碱杆菌属,更准确地说归属于类产碱菌;归属于假单胞菌属,更准确地说归属于Pseudomonas methanica;归属于棒状杆菌属类;归属于芽孢杆菌属类,更准确地说归属于多粘芽孢杆菌;
-归属于汉逊氏酵母属类的酵母如Hansenula capsulata。
除了本发明所使用的碳源和淀粉酶外,对每一种微生物来说,发酵介质和发酵条件都已在一些文献中有所叙述。如在l′ouvrage Chemicals by fermentation-Sydney J.Gutcho-Noyes Data Corp-1973中对适宜的发酵介质作了描述。
典型的含水发酵介质,除了碳源外,还含有有机氮源和/或无机氮源,如玉米(CSL)和/或大豆的可溶提取物、酵母、胨、明胶、酪蛋白的提取物,铵盐如氯化铵、硝酸铵、碳酸铵、硫酸铵,硝酸盐如硝酸钠或硝酸钾。而且发酵介质还可以含有可同化的磷源,它们如以PO3- 4离子形式在开始或在发酵过程中调整PH时加入,还有镁源,如硫酸镁、醋酸镁、氯化镁、硝酸镁、以及对于生长和繁殖至关重要的微量元素,其种类取决于所使用的微生物的来源。
实施该方法的具体方式,可以参照现有的文献,尤其是有关制备呫吨胶的专利文献中所叙述的方法。在大多数情况下,借助上述许多种类微生物制备多糖的细节与制备呫吨胶的细节都是很相似的。
就一般方法而论,其微生物以本身已知的方式和如借助在20升的实验室发酵罐中得到的中间培养物加入发酵介质中,而这些中间培养物本身是由如一升锥瓶中进行接种而得到的。
如在法国专利FR-A-2414555中描述了所有技术人员都知道的接种物或中间培养物的制备方法。
然后,在通空气的介质中并在生长和生产的一个或几个阶段中搅拌数天进行发酵。生长介质和生产介质的组成可以是相同的,也可以是不相同的。为了产生可接受的百分比例的多糖,需要的培养温度和时间自然随所用微生物而改变。其温度一般在约30℃±10℃,在大多数情况下,PH保持在6.0至7.5范围内,最好是在6.5至7.2范围内。人们可以在介质中加入PH调节剂。如需要的话加入如苏打、苛性钾、氢氧化铵等碱性试剂。然而在某些情况下,在较低的PH范围内其产率可能是最佳的。例如,在生产硬葡聚糖(Scléroglucane)时,其起始的PH为3.5至5.5范围内其产率是最佳的(FR-A-1386287)。
为了达到快速发酵的目的,最重要的是搅拌中应往介质通入足够量的空气,以提供使细菌生长的细菌培养液所需用的正确氧量。为了达到发酵和传递氧的条件,需要以惯用方式进行需氧发酵。在这一方面,将看到本发明方法适应于乳化介质中发酵,如EP-A-58364、EP-A-98474、EP-A-187092中所描述的。
发酵完成后,含多糖的糖汁按本身已知方法处理。一般采用巴斯德灭菌法杀死微生物细胞。如果希望这样处理,其糖汁经热处理和/或酶处理和/或予过滤处理以改善其流体性质,以及其澄清与过滤的性能。在一定的情况下,它还具有可以用所有常规方法对其汁进行浓缩的优点。
可用一切可用的方法从糖汁中分离出多糖来。如借助一种对其产品是不可溶的溶剂进行沉淀,例如低级醇,最好是异丙醇,和/或借助常见的无机盐。然后将沉淀的多糖进行过滤、干燥和磨碎。
所述的方法很显然可以间断进行,也可以往发酵罐中连续引入贫介质而连续进行。
人们可以理解如上描述的制备生物聚合物的特定方法。该方法是在能使淀粉或其降解产物分解成单糖和双糖的酶存在下,在含有由淀粉产生的碳水化合物源的介质中,由微生物发酵而制得的。并且发明本身不受发酵介质中具体化合物的限制,也不受特定实施方式的限制。
全部的发酵培养基和多糖粉末都可以在所有已知的水解胶体的应用中加以利用。用稀释糖汁或通过溶解其粉末所得到的含水溶液显示出的流体性质,比用以前的已知方法由未加工淀粉或液化淀粉得到的一种多糖,稀释到相同浓度时的流体性质还要好。
下面实例说明本发明:
实例1
接种物的制备:
在搅拌的小瓶中,把保持在管内的琼脂上的黄单胞菌属野菇菌素(Xanthomonas Campestris)接种到100毫升含酵母提取液、大麦芽提取液、细胞胨和10克/升小麦淀粉的培养介质中。灭菌后的接种介质在28℃培养24小时,瓶中之物用于接种15升发酵介质。
流体未加工淀粉的制备
制备一种含30%(干基重量)的小麦淀粉的乳状液。其PH调正到7,并按占干料表示的淀粉重量0.15%的比例加入流化酶(TERMAMYL 120L -NOVO INDUSTRY)。温度调到85℃,并保持在该温度达30分钟。流体淀粉在121℃灭菌30分钟。
发酵
试验A
在20升发酵罐中,制备15升具有下列组成的贫生产介质:
淀粉(上述制备的) 45克/升(以干料计)
大豆粉 5.1克/升
MgSO4·7H2O 0.25克/升
蒸馏水 适宜至1升
PH调整到7
其温度调正到28℃,用自动添加苏打方式以保持PH在6.8-7.0。当介质的粘度开始增加时,注入的空气量由起始的通气量40VVH上升到55VVH。其介质用3级Rushton浆叶搅拌,其速度为200至400转/分。
当不再剩余糖时停止发酵,其糖汁用巴斯德灭菌法消毒,然后加异丙醇沉淀多糖,并将其过滤,然后在120℃干燥30分钟。
试验B(对照)
除了在生产介质中不加葡糖淀粉酶外,其他均与试验A条件相同的情况下进行试验。当残留糖的浓度不再变化时停止发酵。
在试验A和B进行的过程中,按一定的时间间隔取出糖汁样品以测定介质中残留的淀粉量。在淀粉酸解后,用高性能的液相色谱进行测定,同时测量介质的粘度(Brookfield粘度计,指针4,30转/分,20℃),其结果示于图1。其中曲线A、A1和B、B1分别表示试验A和B的残留淀粉量(克/升)(S)和介质粘度(mpa.S)(V)与发酵时间(D)(小时)的函数关系,其发酵结果列于后:
试验A 试验B
发酵时间 50小时 >66小时
发酵结束时残留的糖 0 >2克/升
可沉淀的干料 31.3克/公斤 29.2克/公斤
未加工淀粉的产率 69.6% 64.9%
由粉末制成浓度为0.2%(在蒸馏水中)的稀水溶液,在各种情况下测得的产品粘度的性能(Brook field粘度计一指针(Aig.)1,20℃)。
试验A 试验B
6转/分 600mpa·s 350mpa·s
30转/分 190mpa·s 135mpa·s
实例2和3
其结果如下:
实例2 实例3
可沉淀的干料 30克/公斤 29.7克/公斤
发酵时间 66小时 50小时
产率/未加工淀粉 66.7% 66%
0.2%溶胶粘度(mpa·s)
6转/分 375 575
30转/分 150 192
实例4
按实例1描述的方法用相同的接种物和在相同条件下制备的流体淀粉进行发酵。
制备的介质具有下述组成:
流体淀粉 100克/升
未加工大豆粉 7.0克/升
MgSO4·7H2O 0.25克/升
蒸馏水 适量至1升
得到下述结果,并与在相同条件下但无葡糖淀粉酶时进行的试验结果进行比较。
实例4 对比例
可沉淀的干料 54克/公斤 49.5克/公斤
发酵时间 130小时 >160小时
发酵结束时残留的糖 0 >15克/升
产率/淀粉 54 49.5
对比试验是不可提取的,并得到高的残留糖,未测定粘度的性能。
Claims (10)
1、一种在含有以淀粉为碳源的含水营养介质中,用微生物需氧发酵生产多糖的方法,其特征在于在至少一种糖化淀粉傅拇嬖谙陆蟹⒔汀?
2、按照权利要求1的方法,其特征在于为了提供占发酵介质量1至15%的葡萄糖而利用必需量的淀粉。
3、按照权利要求1或2的方法,其特征在于所述淀粉选用流体淀粉和淀粉糖汁。
4、按照权利要求1或2的方法,其特征在于所述淀粉是未加工淀粉。
5、按照权利要求4的方法,其特征在于液化酶是按糖化酶加入的。
6、按照权利要求1至5中任何一个权利要求的方法,其特征在于所述的糖化酶选用α淀粉酶、β淀粉酶、葡糖淀粉酶、异淀粉酶、支链淀粉酶及其它们的混合物。
7、按照权利要求1至6中任何一个权利要求的方法,其特征在于为了提供每克干料淀粉具有0.02至4酶的活度单位,要使用足够量的糖化酶。
8、按照权利要求1至7中任何一个权利要求的方法,其特征在于糖化酶是一种葡糖淀粉酶,其使用量占淀粉中含有固体重量的0.01-2%,最好是在0.05至1%之间。
9、按照权利要求7的方法,其特征在于为了提供所用的每克淀粉具有0.1至2酶的活度单位,要使用足够量的糖化酶。
10、按照权利要求1至9中任何一个权利要求的方法,其特征在于所述的微生物选用由黄单胞菌属类、产碱杆菌属类、土壤杆菌属类、节菌属类、固氮菌属类、假单胞菌属类、棒状杆菌属类、 类、小菌核属类的细菌和汉逊酵母属类的酵母。
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR8716855A FR2624135B1 (fr) | 1987-12-04 | 1987-12-04 | Procede de production de polysaccharides |
FR8716855 | 1987-12-04 |
Publications (2)
Publication Number | Publication Date |
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CN1035131A true CN1035131A (zh) | 1989-08-30 |
CN1058753C CN1058753C (zh) | 2000-11-22 |
Family
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CN88109243A Expired - Fee Related CN1058753C (zh) | 1987-12-04 | 1988-12-03 | 多糖的生产方法 |
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US (1) | US5610037A (zh) |
EP (1) | EP0319372B1 (zh) |
JP (1) | JPH0630600B2 (zh) |
KR (1) | KR960002873B1 (zh) |
CN (1) | CN1058753C (zh) |
AT (1) | ATE92532T1 (zh) |
AU (1) | AU617727B2 (zh) |
BR (1) | BR8806349A (zh) |
CA (1) | CA1340727C (zh) |
DE (1) | DE3882932T2 (zh) |
DK (1) | DK672688A (zh) |
ES (1) | ES2059553T3 (zh) |
FR (1) | FR2624135B1 (zh) |
IE (1) | IE61220B1 (zh) |
MX (1) | MX169586B (zh) |
NZ (1) | NZ227160A (zh) |
ZA (1) | ZA888962B (zh) |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
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CN104388493A (zh) * | 2014-11-30 | 2015-03-04 | 内蒙古阜丰生物科技有限公司 | 一种提高黄原胶生产转化率的方法 |
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ATE126538T1 (de) * | 1989-04-12 | 1995-09-15 | Zeneca Ltd | Polymer-herstellung. |
JP2855600B2 (ja) * | 1993-11-08 | 1999-02-10 | 信越化学工業株式会社 | キサンタンガムの発酵生産方法 |
US6268493B1 (en) | 1998-08-07 | 2001-07-31 | Center For The Application Of Molecular Biology To International Agriculture | Preparation of cellobiuronic acid from polysaccharide |
BRPI0406309F1 (pt) * | 2004-11-05 | 2021-03-23 | Empresa Brasileira De Pesquisa Agropecuaria Embrapa Clima Temperado | processo de produção de biopolímero tipo xantana, biopolímero obtido, seus usos; meio de cultura para crescimento de xanthomonas e uso da mesma para produção de biopolímero |
WO2007061102A1 (ja) | 2005-11-28 | 2007-05-31 | Biomedical Research Group Inc. | 発酵及び培養方法、植物発酵エキス、植物発酵エキス配合物、リポ多糖製造方法並びにリポ多糖 |
KR100892359B1 (ko) * | 2008-05-13 | 2009-04-08 | (주)큐젠바이오텍 | 감귤박을 탄소원으로 첨가한 배지에서 스클레로티움 속의 배양을 통한 스클레로글루칸의 제조방법 |
BRPI0804835A2 (pt) * | 2008-11-06 | 2011-05-24 | Quantas Biotecnologia S.A. | processo industrial contìnuo para produção de polissacarìdeo sob a forma de caldo concentrado base água |
JP5860480B2 (ja) | 2011-01-11 | 2016-02-16 | キャプシュゲル・ベルジウム・エヌ・ヴィ | プルランを含む新しい硬カプセル |
TWI639388B (zh) * | 2016-10-26 | 2018-11-01 | 財團法人食品工業發展研究所 | 製備減糖果汁的方法 |
EP3610028A1 (en) | 2017-04-14 | 2020-02-19 | Capsugel Belgium NV | Process for making pullulan |
US11576870B2 (en) | 2017-04-14 | 2023-02-14 | Capsugel Belgium Nv | Pullulan capsules |
CN110904171A (zh) * | 2019-12-31 | 2020-03-24 | 内蒙古阜丰生物科技有限公司 | 低酒精残留黄原胶产品的制备工艺 |
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US3427226A (en) * | 1966-01-27 | 1969-02-11 | Kelco Co | Process for preparing polysaccharide |
US3868307A (en) * | 1971-10-15 | 1975-02-25 | Hiram Walker & Sons Inc | Production of distillers yeast |
US4032403A (en) * | 1974-07-17 | 1977-06-28 | Kabushiki-Kaisha Hayashibara Selbutsukagaku Kenkyujo | Process for the production of saccharified starch products wherein maltose is the predominant constituent |
DE2560532C2 (zh) * | 1974-11-26 | 1988-11-10 | Takeda Chemical Industries, Ltd., Osaka, Jp | |
US4186025A (en) * | 1975-09-25 | 1980-01-29 | Merck & Co., Inc. | Aqueous polysaccharide composition |
FR2328770A1 (fr) * | 1975-10-23 | 1977-05-20 | Santerre Orsan | Nouveau procede de production d'un polysaccharide par fermentation |
US4230806A (en) * | 1977-06-07 | 1980-10-28 | Mitsui Engineering & Shipbuilding Co., Ltd. | Process for the production of microbial protein and lipid from vegetable carbohydrates by culture of microbes |
US4251633A (en) * | 1979-06-11 | 1981-02-17 | Orlowski David C | Multi-stage continuous system for production of heteropolysaccharides |
US4316956A (en) * | 1980-02-06 | 1982-02-23 | Novo Industri A/S | Fermentation process |
US4355106A (en) * | 1981-01-12 | 1982-10-19 | George Weston Limited | Continuous process for the production of gelable exopolysaccharide |
JPS59203498A (ja) * | 1983-05-02 | 1984-11-17 | Nakano Vinegar Co Ltd | 酸性ヘテロ多糖類am−2 |
FR2551087B1 (fr) * | 1983-08-30 | 1986-03-21 | Rhone Poulenc Spec Chim | Procede de traitement d'une solution de polysaccharide et son utilisation |
GB8333797D0 (en) * | 1983-12-19 | 1984-01-25 | Searle & Co | Starch utilization |
JPS6192592A (ja) * | 1984-10-12 | 1986-05-10 | Norin Suisansyo Shokuhin Sogo Kenkyusho | 分岐サイクロデキストリンの製造方法 |
US5175278A (en) * | 1985-06-28 | 1992-12-29 | Merck & Co., Inc. | Heteropolysaccharide S-657 |
US4868293A (en) * | 1985-08-06 | 1989-09-19 | Getty Scientific Development Company | Polysaccharide polymer made by xanthomonas |
AU611159B2 (en) * | 1987-03-06 | 1991-06-06 | Board Of Regents, The University Of Texas System | Microbial cellulose modified during synthesis |
-
1987
- 1987-12-04 FR FR8716855A patent/FR2624135B1/fr not_active Expired - Lifetime
-
1988
- 1988-11-23 ES ES88402930T patent/ES2059553T3/es not_active Expired - Lifetime
- 1988-11-23 AT AT88402930T patent/ATE92532T1/de not_active IP Right Cessation
- 1988-11-23 DE DE88402930T patent/DE3882932T2/de not_active Expired - Lifetime
- 1988-11-23 EP EP88402930A patent/EP0319372B1/fr not_active Expired - Lifetime
- 1988-11-30 ZA ZA888962A patent/ZA888962B/xx unknown
- 1988-12-01 NZ NZ227160A patent/NZ227160A/en unknown
- 1988-12-02 IE IE361488A patent/IE61220B1/en not_active IP Right Cessation
- 1988-12-02 CA CA000584782A patent/CA1340727C/fr not_active Expired - Fee Related
- 1988-12-02 DK DK672688A patent/DK672688A/da not_active Application Discontinuation
- 1988-12-02 BR BR888806349A patent/BR8806349A/pt not_active IP Right Cessation
- 1988-12-02 MX MX026509A patent/MX169586B/es unknown
- 1988-12-02 JP JP63304256A patent/JPH0630600B2/ja not_active Expired - Lifetime
- 1988-12-03 KR KR1019880016130A patent/KR960002873B1/ko not_active IP Right Cessation
- 1988-12-03 CN CN88109243A patent/CN1058753C/zh not_active Expired - Fee Related
- 1988-12-05 AU AU26548/88A patent/AU617727B2/en not_active Ceased
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1995
- 1995-01-27 US US08/379,111 patent/US5610037A/en not_active Expired - Lifetime
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN104388493A (zh) * | 2014-11-30 | 2015-03-04 | 内蒙古阜丰生物科技有限公司 | 一种提高黄原胶生产转化率的方法 |
CN104388493B (zh) * | 2014-11-30 | 2017-07-04 | 内蒙古阜丰生物科技有限公司 | 一种提高黄原胶生产转化率的方法 |
Also Published As
Publication number | Publication date |
---|---|
US5610037A (en) | 1997-03-11 |
FR2624135A1 (fr) | 1989-06-09 |
CN1058753C (zh) | 2000-11-22 |
EP0319372B1 (fr) | 1993-08-04 |
JPH029385A (ja) | 1990-01-12 |
KR890010208A (ko) | 1989-08-07 |
EP0319372A1 (fr) | 1989-06-07 |
NZ227160A (en) | 1991-06-25 |
JPH0630600B2 (ja) | 1994-04-27 |
DK672688D0 (da) | 1988-12-02 |
AU2654888A (en) | 1989-06-08 |
ZA888962B (en) | 1989-08-30 |
KR960002873B1 (ko) | 1996-02-27 |
FR2624135B1 (fr) | 1990-04-13 |
DE3882932T2 (de) | 1994-02-24 |
ES2059553T3 (es) | 1994-11-16 |
ATE92532T1 (de) | 1993-08-15 |
DE3882932D1 (de) | 1993-09-09 |
DK672688A (da) | 1989-06-05 |
IE883614L (en) | 1989-06-04 |
MX169586B (es) | 1993-07-13 |
CA1340727C (fr) | 1999-09-07 |
IE61220B1 (en) | 1994-10-19 |
AU617727B2 (en) | 1991-12-05 |
BR8806349A (pt) | 1989-08-22 |
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