CN114875086A - 一种高品质l-茶氨酸发酵、提取及饲料制作的方法 - Google Patents
一种高品质l-茶氨酸发酵、提取及饲料制作的方法 Download PDFInfo
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- DATAGRPVKZEWHA-UHFFFAOYSA-N L-gamma-glutamyl-n-ethylamine Natural products CCNC(=O)CCC(N)C(O)=O DATAGRPVKZEWHA-UHFFFAOYSA-N 0.000 title claims abstract description 78
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Abstract
本发明属于L‑茶氨酸生产技术领域,公开了一种高品质L‑茶氨酸发酵提取及饲料制作的方法,包括:L‑茶氨酸发酵、微膜过滤、连续离交柱离交、超滤脱色、色谱分离、反渗透、四效蒸发、结晶、干燥、包装等工艺得到精品L‑茶氨酸产品。本发明方法易操作且可连续***化生产,工艺废料经过综合处理可以生产蛋白饲料,全发酵液有效利用,有效的回收了资源,减轻了环保压力。
Description
技术领域
本发明属于L-茶氨酸生产技术领域,具体涉及到一种新的L-茶氨酸的发酵提取工艺及废弃料液制作饲料的方法。
背景技术
L-茶氨酸(L-Theanine),又名谷氨酸γ-乙基酰胺,是茶叶中特有的游离氨基酸,占茶叶总游离氨基酸50 %以上。作为茶叶甘甜味道的主要组成部分,茶氨酸在一定程度上决定着茶叶的质量。茶氨酸具有对人体健康的许多有益作用,包括促进大脑的学习和记忆功能,预防心血管疾病,抑制脂肪积累,安神镇静药物,在食品工业中可以作为茶饮料的品质改良剂、改善食品风味的添加剂和功能食品的添加剂,抑制食品中的苦味和辣味,减轻涩味,因此已被广泛应用于制药和食品行业,成为了茶叶保健成分研究中备受瞩目注目的化合物。
目前,茶氨酸主要是从茶叶或茶叶废渣中提取,普遍存在提取步骤繁琐、有机溶剂使用较多、提取收率和产品纯度低等问题,不能满足大规模生产需求。微生物发酵法以廉价的碳源和氮源为底物,通过微生物菌体代谢,借助自身产茶氨酸的能力,通过葡萄糖发酵直接合成茶氨酸。发酵法原料来源成本相对较低,发酵反应条件较温和,生产工艺相对稳定,可控程度高,容易大规模放大生产,因而成为目前生产茶氨酸的主要方法。
但是,我国目前发酵法生产茶氨酸技术条件不成熟,L-茶氨酸工业生产也常常会受到生产成本的制约,而在生产成本的构成中,分离提取等下游工程的成本占有相当的比例。因此,迫切需要新的技术突破和生产工艺,在提高茶氨酸的转化率的同时降低生产成本。
发明内容
为解决上述问题,克服现有技术的不足之处,本发明提供了一种新的L-茶氨酸的发酵提取工艺,该工艺发酵效率高、易操作,能够实现废物利用,并且合理配置菌株,大大提高了发酵效率。
本发明的目的是通过下述技术方案实现的:
一种高品质L-茶氨酸发酵、提取及饲料制作的方法,其包括如下步骤:L-茶氨酸发酵、微膜过滤、连续离交柱离交和超滤脱色、色谱分离、反渗透、四效蒸发、结晶和烘干、制备饲料。
具体地,所述方法包括如下步骤:
步骤1) L-茶氨酸发酵:将大肠埃希氏菌CGMCC No.23583种子液接入到含有发酵培养基的发酵罐中进行发酵,得到L-茶氨酸发酵液;
步骤2) 微膜过滤:将步骤1)所得L-茶氨酸发酵液加热至70℃打入提取罐,用盐酸调节调pH值为4~5,经微滤膜过滤得到截留物和滤过后的滤液;
步骤3) 连续离交柱离交和超滤脱色:将步骤2)所得滤液经过连续串联离子交换柱,得到L-茶氨酸浓液;然后用盐酸调节L-茶氨酸浓液的pH值为3~4,最后进行超滤膜过滤得到L-茶氨酸超滤液和含有色素及蛋白的浓缩液;
步骤4) 色谱分离:将步骤3)所得L-茶氨酸超滤液泵入色谱***,进行L-茶氨酸和其他杂质的分离,得到纯度更高的L-茶氨酸提取液;
步骤5)反渗透:将步骤4)所得L-茶氨酸提取液进行反渗透膜脱水浓缩,得到纯水和L-茶氨酸料液;
步骤6) 四效蒸发:将步骤5)所得L-茶氨酸料液泵入四效蒸发器进行真空浓缩得到L-茶氨酸浓缩液;
步骤7)结晶和烘干:将步骤6)所得L-茶氨酸浓缩液进行冷却结晶,离心、烘干得到L-茶氨酸产品;
步骤8)制备饲料:将步骤2)所得截留物、步骤3)所得含有色素及蛋白的浓缩液以及步骤5)所得纯水合并得到废弃料液,然后往废弃料液中添加豆粕、酒糟、水稻秸秆粉以及麦麸,1500rpm搅拌20min,通入蒸汽升温至95℃,蒸馏40分钟;最后将蒸馏物烘干,粉碎机粉碎制得饲料。
优选地,所述发酵培养基的组分为:葡萄糖30g/L,甘油30g/L,玉米浆20g/L,七水硫酸镁1g/L,磷酸二氢钾2g/L,磷酸氢二钾2g/L,七水硫酸亚铁50mg/L,一水硫酸镁40mg/L,硫酸锌10mg/L,六水硝酸钴5mg/L。
优选地,所述微滤膜截留分子量为5000Da,微滤温度为40℃,工作压力:进压为2.0bar,出压为1bar。
优选地,所述超滤膜的截留分子量为600-1000Da,操作温度45℃,压力为0.15Mpa。
本发明的技术方案具有以下突出优点及独特性 :
1、本发明菌株发酵效率高,发酵成本低廉,采用连续离交提取L-茶氨酸,其生产工艺简洁,便于操作和维护,占地面积小,可连续性工业生产。
2、本发明采用四效蒸发,蒸发过程在真空作用下,既保证了物料的卫生要求,同时保证了环保要求,同时大大降低了蒸发温度,节约了生蒸汽。
3、本发明设备可配置自动化***,实现进料量自动控制,加热温度自动控制,出料浓度自动控制,清洗自动控制,还可配备突发停电、故障时对敏感性物料的保护措施。其它安全、报警等自动化操作、控制。
4、本发明采用超滤脱色技术,脱色过程相对,脱色效果更好。与传统活性炭脱色所产生大量工业废水和活性炭废料相比,减轻水的使用量,节省了成本。
5、本发明在提取L-茶氨酸过程中,对菌体蛋白等进行回收利用,大大减少了废水外排,避免废液对环境造成的污染,绿色环保;而且从中获取营养丰富的菌体蛋白饲料,有效的回收资源,实现废弃物的资源化利用。
具体实施方式
为了使本技术领域的人员更好地理解本申请中的技术方案,下面将结合本申请具体实施例,对本技术方案进行完整地描述。
实施例1
大肠埃希氏菌(Escherichia coli)CTh2020-05,其于2021年10月12日保藏于中国微生物菌种保藏管理委员会普通微生物中心(简称CGMCC,地址:北京市朝阳区北辰西路1号院3号,中国科学院微生物研究所,邮编100101),保藏号为CGMCC No.23583。
样品采集于生产车间L-茶氨酸发酵废渣,48℃热水处理3min,升温至50℃继续处理3min,然后涂布LB固体培养基,38℃培养24h收集菌斑,挑选L-茶氨酸表达量最高的菌株XFM-7;采用微生物菌种鉴定Biology仪鉴定,鉴定结果为大肠埃希氏菌。采用常压室温等离子体技术进行诱变,筛选L-茶氨酸表达量最高的菌株,即为大肠埃希氏菌(Escherichiacoli)CTh2020-05。
实施例2
一种发酵生产L-茶氨酸的方法,具体操作步骤如下:
1)将大肠埃希氏菌(Escherichia coli)CTh2020-05菌种接入葡萄糖30g/L,七水硫酸镁0.5g/L,酵母粉6g/L,磷酸二氢钾2g/L,柠檬酸2g/L,蛋白胨2g/L,七水硫酸亚铁10mg/L,一水硫酸镁10mg/L,硫酸锌6.5mg/L,六水硝酸钴5mg/L的种子培养基中,用氨水调节pH至4.5,温度121-123℃,时间25min,进行实消灭菌。灭菌后用冷凝水降温至38℃,控制pH 6.8~7.2、压力0.05MPa、溶氧控制为30%-50%,培养8h,得到种子液。
2)将步骤1)得到的种子液稀释50倍测得OD=0.4时开始移种,接种量为12.5%,接入到含有发酵培养基(发酵培养基:葡萄糖60g/L,玉米浆20g/L,七水硫酸镁1g/L,磷酸二氢钾2g/L,磷酸氢二钾2g/L,七水硫酸亚铁50mg/L,一水硫酸镁40mg/L,硫酸锌10mg/L,六水硝酸钴5mg/L)的发酵罐中进行发酵,测得OD=0.3时开始补加乙胺,初期流加速率为1mL/h.L,4h后增加到2mL/h.L。通过流加质量浓度为70%的葡萄糖溶液控制含糖量不低于1%(质量百分比)。控制发酵过程中搅拌转速: 550rpm,pH=7.0,压力0.05MPa,温度36-40℃,溶氧控制为20%,发酵24h,收集发酵液。
实施例3
不同发酵温度对发酵产L-茶氨酸的影响。
发酵工艺参照实施例2,发酵液中L-茶氨酸产量见表1:
表1
菌株 | 36℃ | 37℃ | 38℃ | 39℃ | 40℃ |
XFM-7 | 31.3 | 35.4 | 35.8 | 33.1 | 27.6 |
CTh2020-05 | 46.8 | 48.9 | 53.2 | 54.0 | 47.9 |
如上表1所示,与出发菌株XFM-7相比较,CTh2020-05发酵产茶氨酸效率提高了约50%,性能优异;并且较常规发酵菌株的最适发酵温度有所提高,有利于减少杂菌污染的可能性。
实施例4
发酵培养基碳源对L-茶氨酸的影响。
基础发酵培养基:碳源60g/L,玉米浆20g/L,七水硫酸镁1g/L,磷酸二氢钾2g/L,磷酸氢二钾2g/L,七水硫酸亚铁50mg/L,一水硫酸镁40mg/L,硫酸锌10mg/L,六水硝酸钴5mg/L。
不同碳源类型对L-茶氨酸的影响。
组1:葡萄糖;组2:葡萄糖:蔗糖=1:1质量比;组3:葡萄糖:甘油=1:1质量比;组4:葡萄糖:乳糖=1:1质量比;组5:蔗糖;组6:甘油。
发酵工艺参照实施例2,发酵温度为39℃,发酵液中L-茶氨酸产量见表2:
表2
菌株 | 组1 | 组2 | 组3 | 组4 | 组5 | 组6 |
XFM-7 | 33.1 | 31.4 | 27.9 | 29.8 | 27.6 | 32.0 |
CTh2020-05 | 54.0 | 52.5 | 57.8 | 53.6 | 45.3 | 51.2 |
如上表2所示,葡萄糖+甘油作为复合碳源的组3,CTh2020-05发酵产茶氨酸的效率最高,较葡萄糖作为碳源的组1提高了约7%,而这种趋势并没有在XFM-7和现有的L-茶氨酸生产用大肠杆菌中体现,葡萄糖是XFM-7菌株等大肠杆菌的最佳发酵碳源。考虑到生物能源领域中甘油大量过剩,成本相对低廉,CTh2020-05菌株利用部分甘油作为碳源,不仅能够提高发酵效率,而且解决了甘油过剩的问题,工业应用价值较高。
实施例5
一种高品质L-茶氨酸提取及饲料制作的方法,其包括如下步骤:
步骤1):发酵工艺参照实施例2;发酵培养基替换为:葡萄糖30g/L,甘油30g/L,玉米浆20g/L,七水硫酸镁1g/L,磷酸二氢钾2g/L,磷酸氢二钾2g/L,七水硫酸亚铁50mg/L,一水硫酸镁40mg/L,硫酸锌10mg/L,六水硝酸钴5mg/L。
步骤2):将步骤1)所得L-茶氨酸发酵液加热至70℃打入提取罐,用盐酸调节调pH值为4.5,经微滤膜过滤得到截留物和滤过后的滤液。所述微滤膜截留分子量为5000Da,微滤温度为40℃,工作压力:进压为2.0bar,出压为1bar。
步骤3):将步骤2)所得滤液经过连续串联离子交换柱,得到L-茶氨酸浓液;然后用盐酸调节L-茶氨酸浓液的pH值为3.5左右,最后进行超滤膜过滤得到L-茶氨酸超滤液和含有色素及蛋白的浓缩液。所述超滤膜的截留分子量为600Da,操作温度45℃,压力为0.15Mpa。
步骤4):将步骤3)所得L-茶氨酸超滤液泵入色谱***,进行L-茶氨酸和其他杂质的分离;柱温:40℃,将L-茶氨酸进行解脱,得到纯度更高的L-茶氨酸提取液。
步骤5):将步骤4)所得L-茶氨酸提取液进行反渗透膜脱水浓缩,得到纯水和L-茶氨酸料液。
步骤6):将步骤5)所得L-茶氨酸料液泵入四效蒸发器进行真空浓缩得到L-茶氨酸浓缩液。
步骤7):将步骤6)所得L-茶氨酸浓缩液进行冷却结晶,离心、烘干得到L-茶氨酸产品;经检测,纯度可达到99.6%。
步骤8):将步骤2)所得截留物、步骤3)所得含有色素及蛋白的浓缩液以及步骤5)所得纯水合并得到废弃料液,然后往废弃料液中添加占废弃料液10%(w/v)豆粕、8%(w/v)酒糟、12%(w/v)水稻秸秆粉以及15%(w/v)麦麸,1500rpm搅拌20min,通入蒸汽升温至95℃,蒸馏40分钟;然后将蒸馏物烘干,粉碎机粉碎制得饲料。
本发明采用连续离交柱离交、超滤脱色、色谱分离、反渗透、四效浓缩等技术,大大提高了L-茶氨酸的成品收率和纯度,有利于工业化,废弃料液制作饲料,实现了清洁生产和资源重复利用。
上述虽然结合实施例对本发明的具体实施方式进行了介绍,但并非对本发明保护范围的限制,所属领域技术人员应该明白,这对本领域技术人员而言应该很明确,在不偏离本发明精神的基础上所做的这些修改或改进,均属于本发明保护的范围。
Claims (5)
1.一种高品质L-茶氨酸发酵、提取及饲料制作的方法,其包括如下步骤:L-茶氨酸发酵、微膜过滤、连续离交柱离交和超滤脱色、色谱分离、反渗透、四效蒸发、结晶和烘干、制备饲料。
2.根据权利要求1所述的方法,其特征在于,所述方法包括如下步骤:
步骤1) L-茶氨酸发酵:将大肠埃希氏菌CGMCC No.23583种子液接入到含有发酵培养基的发酵罐中进行发酵,得到L-茶氨酸发酵液;
步骤2) 微膜过滤:将步骤1)所得L-茶氨酸发酵液加热至70℃打入提取罐,用盐酸调节调pH值为4~5,经微滤膜过滤得到截留物和滤过后的滤液;
步骤3) 连续离交柱离交和超滤脱色:将步骤2)所得滤液经过连续串联离子交换柱,得到L-茶氨酸浓液;然后用盐酸调节L-茶氨酸浓液的pH值为3~4,最后进行超滤膜过滤得到L-茶氨酸超滤液和含有色素及蛋白的浓缩液;
步骤4) 色谱分离:将步骤3)所得L-茶氨酸超滤液泵入色谱***,进行L-茶氨酸和其他杂质的分离,得到纯度更高的L-茶氨酸提取液;
步骤5)反渗透:将步骤4)所得L-茶氨酸提取液进行反渗透膜脱水浓缩,得到纯水和L-茶氨酸料液;
步骤6) 四效蒸发:将步骤5)所得L-茶氨酸料液泵入四效蒸发器进行真空浓缩得到L-茶氨酸浓缩液;
步骤7)结晶和烘干:将步骤6)所得L-茶氨酸浓缩液进行冷却结晶,离心、烘干得到L-茶氨酸产品;
步骤8)制备饲料:将步骤2)所得截留物、步骤3)所得含有色素及蛋白的浓缩液以及步骤5)所得纯水合并得到废弃料液,然后往废弃料液中添加豆粕、酒糟、水稻秸秆粉以及麦麸,1500rpm搅拌20min,通入蒸汽升温至95℃,蒸馏40分钟;最后将蒸馏物烘干,粉碎机粉碎制得饲料。
3.根据权利要求2所述的方法,其特征在于,所述发酵培养基的组分为:葡萄糖30g/L,甘油30g/L,玉米浆20g/L,七水硫酸镁1g/L,磷酸二氢钾2g/L,磷酸氢二钾2g/L,七水硫酸亚铁50mg/L,一水硫酸镁40mg/L,硫酸锌10mg/L,六水硝酸钴5mg/L。
4.根据权利要求2所述的方法,其特征在于,所述微滤膜截留分子量为5000Da,微滤温度为40℃,工作压力:进压为2.0bar,出压为1bar。
5.根据要求2所述的工艺,其特征在于,所述超滤膜的截留分子量为600-1000Da,操作温度45℃,压力为0.15Mpa。
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