CN116554543A - 一种固定化介质及其制备方法与应用 - Google Patents
一种固定化介质及其制备方法与应用 Download PDFInfo
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- CN116554543A CN116554543A CN202310607150.8A CN202310607150A CN116554543A CN 116554543 A CN116554543 A CN 116554543A CN 202310607150 A CN202310607150 A CN 202310607150A CN 116554543 A CN116554543 A CN 116554543A
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- fermentation
- tubular reactor
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- tank
- reaction
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- YMWUJEATGCHHMB-UHFFFAOYSA-N Dichloromethane Chemical compound ClCCl YMWUJEATGCHHMB-UHFFFAOYSA-N 0.000 claims description 24
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- BAUYGSIQEAFULO-UHFFFAOYSA-L iron(2+) sulfate (anhydrous) Chemical compound [Fe+2].[O-]S([O-])(=O)=O BAUYGSIQEAFULO-UHFFFAOYSA-L 0.000 description 1
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- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
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Abstract
本发明公开了一种固定化介质及其制备方法与应用。本发明的固定化介质是将多羟基纤维素粉碎过筛后,加入到含有聚氨酯发泡催化体系的反应釜中反应得到聚氨酯泡沫复合材料,再将反应得到的聚氨酯泡沫复合材料经化学修饰处理后烘干得到的。本发明通过对上述催化体系和化学修饰处理过程进行优化,使得聚氨酯泡沫复合材料的拉伸强度和柔韧性得到了显著提升,同时,增强了纤维之间以及纤维与聚氨酯泡沫复合材料的结合力。在利用改进后的固定化介质进行酵母发酵产乙醇的应用中,通过改进管式反应器和发酵条件,提高了固定化介质装填密度,实现了自动化连续发酵生产,降低了生产风险,提高了设备利用率。同时,可进行高浓度发酵,大幅降低了蒸馏过程能耗。
Description
技术领域
本发明属于工业生物技术领域,具体涉及一种固定化介质及其制备方法与应用。
背景技术
利用固定化技术产燃料乙醇的研究已有相当久的历史。采用固定化细胞发酵具有发酵速率快、糖醇转化率高以及生产稳定等优点。传统的固定化技术以凝胶包埋技术和表面吸附技术为主。凝胶包埋技术用角叉莱胶、卡拉胶、海藻酸钙、海藻酸钠等对细胞进行固定发酵。此类包埋载体具有成型方便及固定化密度高等优点,但其机械强度低,传质弱,抗微生物分解能力较差;同时因传质限制,难以实现细胞自我更新。吸附法中的吸附材料有陶瓷、活性炭、各种纤维类及其改性形式材料,由于材料密度高或者分散性不好,导致载体接触面不够理想,影响了固定化发酵效率。由于传统固定化技术种种缺陷,研究仅停留于小中试试验水平,未曾有应用层面的突破。
发明内容
本发明所要解决的技术问题是针对现有技术的不足,提供一种经过催化和化学修饰的固定化介质及其制备方法与在酵母发酵产乙醇中的应用。
为了解决上述技术问题,本发明采用的技术方案如下:
一种固定化介质的制备方法,将多羟基纤维素粉碎过筛后,通过压缩氦气或氮气加入到含有聚氨酯发泡催化体系的反应釜中反应得到聚氨酯泡沫复合材料,再将反应得到的聚氨酯泡沫复合材料经化学修饰处理后,烘干得到固定化介质。
其中,所述的多羟基纤维素为细菌纤维素、植物纤维和人工合成纤维中的任意一种或几种的组合,优选细菌纤维素。
具体的,所述的细菌纤维素,其聚合度为600-2000,其质量为50-200g;优选的,聚合度为1600,质量为110g。
其中,所述的聚氨酯发泡催化体系中原料配比按质量份数算包括:100-150份异氰酸酯,80-200份聚醚多元醇,1-5份发泡剂,0.1-1份催化剂,0.5-10份阻燃剂;优选的,聚氨酯发泡催化体系中原料配比按质量份数算包括:120份异氰酸酯,150份聚醚多元醇,1份发泡剂,0.2份催化剂,0.5份阻燃剂。
具体的,所述的异氰酸酯为二苯基甲烷二异氰酸酯、二环己基甲烷二异氰酸酯、六亚甲基二异氰酸酯、赖氨酸二异氰酸酯和异佛尔酮二异氰酸酯中的任意一种或几种的组合;所述的聚醚多元醇为官能团数3-8,分子量为1500-4000的聚醚多元醇;所述的发泡剂为二氯甲烷和水中的任意一种或两种的组合,优选二氯甲烷和水的混合物,二者体积比为1:0.5-2;所述的催化剂为胺类物质,为三乙烯二胺或聚乙烯亚胺,优选三乙烯二胺;所述的阻燃剂为甲基膦酸二甲酯。
其中,所述的反应,其反应条件为:温度25-40℃,时间5-30分钟,当反应釜内体系发白及不再有气泡生成时,反应结束。
其中,所述的化学修饰处理,是将聚氨酯泡沫复合材料浸泡于修饰剂中。
具体的,所述的化学修饰处理,具体是将聚氨酯泡沫复合材料浸泡于50-200mL/L修饰剂水溶液中,35-80℃条件下浸泡处理1-6个小时,pH=4-7;优选的,将聚氨酯泡沫复合材料浸泡于80mL/L修饰剂水溶液中,35-65℃条件下浸泡处理5个小时,pH=4-7。
其中,所述的修饰剂为甲醛、戊二醛和苯甲醛中的任意一种或几种的组合,优选为戊二醛。
其中,所述的粉碎过筛,其目数为80-200目,优选目数为100目。
上述固定化介质的制备方法制备得到的固定化介质也在本发明所保护的范围之内。
上述固定化介质在酵母发酵产乙醇中的应用也在本发明所保护的范围之内。
其中,所述的酵母发酵产乙醇,其装置包括管式反应器1、缓冲罐3、循环泵4和发酵罐5;物料进口与所述的管式反应器1的进口串联,所述的管式反应器1的出口与缓冲罐3、循环泵4串联后再通过管道回流至所述的管式反应器1的进口,所述的管式反应器1的出口分别独立地与多个发酵罐5串联,多个发酵罐5之间并联设置。
具体的,所述的多个发酵罐,其数量为2-10个,优选8个。
其中,所述的酵母发酵产乙醇,先进行酵母种子液的固定化培养,再进行间歇式发酵产乙醇。
上述酵母种子液的固定化培养,具体步骤如下:将所述的固定化介质填充于管式反应器1内,将酵母种子液通过物料进口流加进管式反应器1中,再从管式反应器1的出口流入缓冲罐3中,待缓冲罐3内的液位达到罐体积的40-70%时,停止加入酵母种子液,打开循环泵4回流至管式反应器1的进口,使得物料循环流经管式反应器1、缓冲罐3和循环泵4,进行酵母种子液的固定化培养。
其中,所述的固定化介质,其装填密度为2-20g/dm3;所述的酵母种子液,其酵母数为2.5-3.2亿个/mL,还原糖浓度为20-150g/L。
其中,所述的固定化培养,其培养条件为:循环流速0.2-0.6m/s,温度29-35℃,当发酵液中菌体浓度达到0.5亿个/mL时,结束固定化培养。
在一些实施例中,将所述的密度为6g/dm3的固定化介质填充于管式反应器1内,打开物料进口的阀门2-1,将酵母数为2.8亿个/mL,还原糖浓度为100g/L的酵母种子液通过物料进口流加进管式反应器1中,再从管式反应器1的出口经阀门2-2流入200L的缓冲罐3中,待缓冲罐3内的液位达到罐体积的50%时,关闭物料进口的阀门2-1,停止加入酵母种子液,打开循环泵4经阀门2-12回流至管式反应器1的进口,使得物料循环流经管式反应器1、阀门2-2、缓冲罐3、循环泵4和阀门2-12,在循环流速0.3m/s-0.5m/s,温度32℃的条件下进行酵母种子液的固定化培养。当发酵液中菌体浓度达到0.5亿个/mL左右时,结束固定化培养。
上述间歇式发酵产乙醇,具体是当固定化培养结束后,排出种子液,关闭缓冲罐3,通过物料进口向所述的管式反应器1流加糖化液,并以相同的流速依次流入多个发酵罐5,进行间歇式发酵。
其中,所述的糖化液为糖蜜水解液、纤维素水解液、淀粉质水解液和合成培养基(合成培养基配方:酵母粉2-10g/L,玉米浆5-20g/L,尿素2-6g/L,硫酸镁0.2-2g/L,磷酸二氢钾0.2-2g/L,硫酸亚铁0.01-0.1g/L)中的任意一种或两种的组合,总糖为200-260g/L。优选的糖化液为淀粉质水解液中的玉米糖化液,其总糖为200g/L或256g/L。其中,玉米糖化液制备过程如下:按玉米和水1:2.5-2.8比例配制,调pH至5.5-6.0,再80-90℃高温处理1-3小时,冷却后调pH至4.5,加入糖化酶,再经过滤去除固体杂质,所得清液即为玉米糖化液。
其中,在向所述的管式反应器1流加糖化液时,通过控制糖化液流速从而控制所述的管式反应器1中发酵残糖的总浓度为30-160g/L,优选120-160g/L。
其中,所述的间歇式发酵,是将经所述的管式反应器1反应后的糖化液,连续流加进入第一发酵罐中进行发酵反应,第一发酵罐中的发酵液加至60-85%v/v目标体积后,将经所述的管式反应器1反应后的糖化液,连续流加进入第二发酵罐中进行发酵反应,以此类推连续流加进入最后一个发酵罐;
具体的,所述的发酵罐中的发酵条件为30-37℃、50-300r/min,当单一发酵罐中的残糖降至7-15g/L或还原糖降至1-3g/L时,该发酵罐发酵结束,流出发酵液收集;
具体的,所述的间歇式发酵,通过控制流速和发酵罐体积以及发酵罐数量,使得最后一个发酵罐中发酵液加至60-85%v/v目标体积后,第一个发酵罐发酵恰好结束;将经所述的管式反应器1反应后的糖化液连续流加进入第一发酵罐中进行发酵反应,依次循环,实现间歇式发酵。
在一些实施例中,当固定化培养结束后,排出种子液,关闭缓冲罐3,通过物料进口向所述的管式反应器1以0.2m/s的流速连续流加总糖浓度为200g/L的玉米糖化液与所述的管式反应器1中固定化培养后的酵母反应,然后将反应后带有酵母的糖化液从管式反应器1中流出,并以相同的流速依次流入8个发酵罐5-1至5-8中。每个发酵罐入料时间约1小时,发酵周期为7小时,发酵温度32℃、发酵转速200r/min。当第一发酵罐5-1中的发酵液加至70%v/v目标体积后,再入料第二发酵罐5-2,直至入料第八发酵罐5-8,此时第一发酵罐中残糖降至12g/L,还原糖降至2g/L,第一发酵罐5-1内发酵反应结束。当第八发酵罐5-8发酵结束,再开始入料第一发酵罐5-1,依次循环,实现间歇式发酵产乙醇。
在一些实施例中,所述的间歇式发酵产乙醇还可以通过串联相同规格的固定好酵母种子的管式反应器1实现乙醇的高浓度发酵。
有益效果:
(1)细菌纤维素增强了聚氨酯泡沫复合材料的强度。通过控制聚合度大小和添加量多少,提高固定化介质的柔韧性和抗张强度;同时,化学修饰增强了纤维之间以及纤维与聚氨酯泡沫复合材料的结合力。
(2)固定化介质表面纤维结构增加了介质比表面积,同时网状结构材料实现了固定化介质在反应体系中的均匀分散性,提高了菌体吸附效率和发酵水平。
(3)管式反应器培养形式最大化提高了固定化介质装填密度,大幅提高了固定化细胞密度,易于实现自动化连续发酵生产。同时,固定化体系小,降低了染菌失败导致的生产风险。另外,固定化种子抗衰老性强,避免了搅拌环境培养易衰老的现象,可长期稳定运行。
(4)设备利用率高。管式反应器可完全取代种子罐,可以实现24小时不间断种子培养。同时,可进行高浓度发酵,大幅降低蒸馏过程能耗。
附图说明
下面结合附图和具体实施方式对本发明做更进一步的具体说明,本发明的上述和/或其他方面的优点将会变得更加清楚。
图1为管式反应器示意图。其中,A:正面截面图、B:侧面截面图。
图2为反应装置流程示意图。其中,管式反应器1、阀门2-1至2-12、缓冲罐3、循环泵4、发酵罐5-1至5-8。
具体实施方式
下述实施例中所述实验方法,如无特殊说明,均为常规方法;所述试剂和材料,如无特殊说明,均可从商业途径获得。
实施例1:聚氨酯泡沫复合材料的制备
向反应釜中分别加入聚氨酯发泡催化体系(聚氨酯发泡催化体系中原料配比按质量份数算包括:120份异氰酸酯,150份聚醚多元醇,1份发泡剂,0.2份催化剂,0.5份阻燃剂)进行反应。即向反应釜中依次加入150g聚醚多元醇、1g发泡剂、0.2g催化剂和0.5g阻燃剂。控制反应温度在38℃,不断搅拌,反应25分钟后,加120g异氰酸酯。
其中,所述的聚醚多元醇可以选用官能团数3-8,分子量为1500-4000的聚醚多元醇,考虑到聚醚多元醇官能团和分子量对反应强度和成品性能都有影响,在官能团相同的情况下,聚醚多元醇的分子量越大,其反应活性越低,但制得的聚氨酯软泡制品的拉伸强度、伸长率以及回弹性则显著提升;在分子量相同的情况下,聚醚多元醇的官能团增加,则反应活性增强,反应速率相对加快,生成聚氨酯的交联度提高,泡沫硬度随之提高,但材料的伸长率却有所下降。因此官能团数5和分子量为2500相对较佳,所以选用官能团数5,分子量为2500的聚醚多元醇;其中,在发泡剂的选用上,考虑到水作为发泡剂,成品密度较大;二氯甲烷是低沸点化合物,作为辅助发泡剂,可以降低成品密度,本发明所述的发泡剂为二氯甲烷与水的混合物,二者体积比为1:1;其中,所述的催化剂可以选用三乙烯二胺或聚乙烯亚胺,二者效果相当,考虑到聚乙烯亚胺催化活性较强,反应相对剧烈,三乙烯二胺反应则相对温和,所以本发明选择三乙烯二胺;其中,所述的异氰酸酯选用二苯基甲烷二异氰酸酯或二环己基甲烷二异氰酸酯中的任意一种。
待再反应2分钟后,将聚合度分别为900和1600的细菌纤维素粉碎过筛(100目)后,分别取筛下物80-140g,通过压缩氦气加入聚氨酯发泡催化体系中,待反应釜内体系发白及不再有气泡生成时,发泡反应结束,获得聚氨酯泡沫复合材料。以质量为110g的植物纤维(棉纤维)和不添加多羟基纤维素的聚氨酯发泡催化体系为对照(表1)。
表1不同多羟基纤维素在不同条件下的催化结果
结果发现,当添加110g的聚合度为1600细菌纤维素,其比棉纤维拉伸强度提高了19.5%,密度提高了10.5%,比表面积高了16%左右;与不添加任何纤维素的成品相比,比表面积提升了31.7%。
实施例2:戊二醛修饰
将实施例1制备的编号为4的聚氨酯泡沫复合材料分别浸泡于80mL/L修饰剂戊二醛水溶液中,用硫酸调pH至4-7。在35-65℃条件下浸泡5个小时,然后用纯水冲洗干净,再进行100℃烘干处理至恒重。以编号6未添加多羟基纤维素的聚氨酯泡沫复合材料为对照。结果发现,编号4和6经化学修饰处理后,其材料的机械强度都得到了显著提升,且比实施例1未进行化学修饰处理的分别高出了27和12%。(表2)
表2不同浸泡条件下聚氨酯泡沫复合材料的拉伸强度
处理条件 | 1 | 2 | 3 | 4 | 5 | 6 | 7 |
复合材料编号 | 4 | 4 | 4 | 4 | 4 | 4 | 6 |
pH | 4 | 4 | 5 | 5 | 6 | 7 | 5 |
温度 | 35 | 50 | 50 | 65 | 50 | 50 | 50 |
拉伸强度KPa | 132.3 | 138.5 | 165.2 | 127.7 | 154.6 | 141.3 | 135.4 |
实施例3:摇瓶吸附实验
将实施例2中化学修饰处理后的2种固定化介质(处理条件3和7)各5g放置于装有200mL酵母种子液的500mL摇瓶,种子液中酵母数为2.5亿个/ml。在转速80r/min、温度30℃的摇床培养6小时,结果发现,处理条件3的吸附量为89.2%,明显高于处理条件7下68.2%的吸附量。
实施例4:种子液固定化
选取直径50cm、长度10m的不锈钢管作为管式反应器1容器,填充满经实施例3摇瓶吸附实验后优选的固定化介质(处理条件3),介质固定在罐内支架表面(装填密度6g/dm3),如图1所示。200L搅拌罐作为缓冲罐3,如图2所示。用0.2g/L的次氯酸钙液体浸泡杀菌整个体系后排空杀菌水,然后用自来水清洗两次。打开物料进口的阀门2-1,将酵母数为2.8亿个/mL,还原糖浓度为100g/L的酵母种子液通过物料进口流加进杀菌后的管式反应器1中,再从管式反应器1的出口经阀门2-2流入杀菌后的缓冲罐3中,待缓冲罐3内的液位达到罐体积的50%时,关闭物料进口的阀门2-1停止加入酵母种子液,打开循环泵4,经阀门2-12回流至管式反应器1的进口,使得物料循环流经管式反应器1、阀门2-2、缓冲罐3、循环泵4和阀门2-12,在循环流速0.3m/s-0.5m/s,温度32℃的条件下进行酵母种子液的固定化培养。当循环培养至发酵液中菌体浓度达到0.5亿个/mL左右,结束固定化培养。结果表明,当循环流速为0.3m/s时,菌体吸附速率比循环流速为0.5m/s条件下快了32%。
实施例5:固定化发酵
当固定化培养结束后,排出种子液,关闭缓冲罐3,通过物料进口向管式反应器1以0.2m/s的流速连续流加玉米糖化液(总糖200g/L),与管式反应器1中固定化培养后的酵母反应,然后将反应后带有0.9亿个/mL酵母数的糖化液(总残糖120g/L)从管式反应器1中流出,并以相同的流速依次流入8个2m3发酵罐5-1至5-8(装液量1500L),如图2所示。每个发酵罐入料时间约1小时,当入料1小时后整个体系酵母浓度约有1.2亿个/mL,发酵周期为7小时,发酵温度32℃、发酵转速200r/min。当第一发酵罐5-1中的发酵液加至70%v/v目标体积后,再入料第二发酵罐5-2,直至入料第八发酵罐5-8,此时第一发酵罐中残糖降至12g/L,还原糖降至2g/L,第一发酵罐5-1内发酵反应结束,放出排料并收集。当第八发酵罐5-8发酵结束后,再开始入料第一发酵罐5-1,依次循环,实现间歇式发酵产乙醇。结果发现,整个发酵体系共运行了35天,各个发酵罐运行稳定,平均乙醇浓度96.2g/L,转化率94.3%。
实施例6:高浓度发酵
将2台同样尺寸规格的固定好酵母种子的管式反应器1串联。通过物料进口向管式反应器1以0.1m/s的流速连续流加玉米糖化液(总糖256g/L),与管式反应器1中固定化培养后的酵母反应,然后将反应后带有1.1亿个/mL酵母数的糖化液(总残糖160g/L)从管式反应器1中流出,并以相同的流速依次流入8个2m3发酵罐5-1至5-8(装液量1500L)。每个发酵罐入料时间约2小时,当入料2小时后整个体系酵母浓度约有1.5亿个/mL,发酵周期为16小时,发酵温度32℃、发酵转速200r/min。当第一发酵罐5-1中的发酵液加至70%v/v目标体积后,再入料第二发酵罐5-2,直至入料第八发酵罐5-8,此时第一发酵罐中残糖降至14g/L,还原糖降至2.9g/L,第一发酵罐5-1内发酵反应结束,放出排料并收集。第八发酵罐5-8发酵结束后,再开始入料第一发酵罐5-1,依次循环,实现间歇式发酵产乙醇。结果发现,高浓度乙醇发酵体系共运行了42天,各个发酵罐运行稳定,平均乙醇浓度122.9g/L,转化率93.9%。以乙醇游离发酵为对照,在相同发酵体系下,相比15%v/v接种量的游离发酵,其发酵周期缩短了34小时,转化率提高2个百分点。
本发明提供了一种固定化介质及其制备方法与应用的思路及方法,具体实现该技术方案的方法和途径很多,以上所述仅是本发明的优选实施方式,应当指出,对于本技术领域的普通技术人员来说,在不脱离本发明原理的前提下,还可以做出若干改进和润饰,这些改进和润饰也应视为本发明的保护范围。本实施例中未明确的各组成部分均可用现有技术加以实现。
Claims (15)
1.一种固定化介质的制备方法,其特征在于,将多羟基纤维素粉碎过筛后,加入到含有聚氨酯发泡催化体系的反应釜中反应得到聚氨酯泡沫复合材料,再将反应得到的聚氨酯泡沫复合材料经化学修饰处理后,烘干得到固定化介质,
其中,所述的聚氨酯发泡催化体系中原料配比按质量份数算包括:100-150份异氰酸酯,80-200份聚醚多元醇,1-5份发泡剂,0.1-1份催化剂,0.5-10份阻燃剂;
其中,所述的化学修饰处理,是将聚氨酯泡沫复合材料浸泡于修饰剂中。
2.根据权利要求1所述的制备方法,其特征在于,所述的多羟基纤维素为细菌纤维素、植物纤维和人工合成纤维中的任意一种或几种的组合,优选细菌纤维素。
3.根据权利要求2所述的制备方法,其特征在于,所述的细菌纤维素,其聚合度为600-2000,其质量为50-200g。
4.根据权利要求1所述的制备方法,其特征在于,所述的粉碎过筛,其目数为80-200目,优选目数为100目。
5.根据权利要求1所述的制备方法,其特征在于,所述的异氰酸酯为二苯基甲烷二异氰酸酯、二环己基甲烷二异氰酸酯、六亚甲基二异氰酸酯、赖氨酸二异氰酸酯和异佛尔酮二异氰酸酯中的任意一种或几种的组合;所述的聚醚多元醇为官能团数3-8,分子量为1500-4000的聚醚多元醇;所述的发泡剂为二氯甲烷和水中的任意一种或两种的组合,优选二氯甲烷和水的混合物,二者体积比为1:0.5-2;所述的催化剂为胺类物质,为三乙烯二胺或聚乙烯亚胺,优选三乙烯二胺;所述的阻燃剂为甲基膦酸二甲酯。
6.根据权利要求1所述的制备方法,其特征在于,所述的反应,其反应条件为:温度25-40℃,时间5-30分钟。
7.根据权利要求1所述的制备方法,其特征在于,所述的化学修饰处理,具体是将聚氨酯泡沫复合材料浸泡于50-200mL/L修饰剂水溶液中,35-80℃条件下浸泡处理1-6个小时,pH=4-7;其中,所述的修饰剂为甲醛、戊二醛和苯甲醛中的任意一种或几种的组合。
8.权利要求1-7任意一项所述的制备方法制备得到的固定化介质。
9.权利要求8所述的固定化介质在酵母发酵产乙醇中的应用。
10.根据权利要求9所述的应用,其特征在于,所述的酵母发酵产乙醇,其装置包括管式反应器(1)、缓冲罐(3)、循环泵(4)和发酵罐(5);物料进口与所述的管式反应器(1)的进口串联,所述的管式反应器(1)的出口与缓冲罐(3)、循环泵(4)串联后再通过管道回流至所述的管式反应器(1)的进口,所述的管式反应器(1)的出口分别独立地与多个发酵罐(5)串联,多个发酵罐(5)之间并联设置。
11.根据权利要求10所述的应用,其特征在于,将权利要求1所述的固定化介质填充于管式反应器(1)内,将酵母种子液通过物料进口流加进管式反应器(1)中,再从管式反应器(1)的出口流入缓冲罐(3)中,待缓冲罐(3)内的液位达到罐体积的40-70%时,停止加入酵母种子液,打开循环泵(4)回流至管式反应器(1)的进口,使得物料循环流经管式反应器(1)、缓冲罐(3)和循环泵(4),进行酵母种子液的固定化培养;
当固定化培养结束后,排出种子液,关闭缓冲罐(3),通过物料进口向所述的管式反应器(1)流加糖化液,并以相同的流速依次流入多个发酵罐(5),进行间歇式发酵。
12.根据权利要求11所述的应用,其特征在于,所述的固定化介质,其装填密度为2-20g/dm3;所述的酵母种子液,其酵母数为2.5-3.2亿个/mL,还原糖浓度为20-150g/L;所述的固定化培养,其培养条件为:循环流速0.2-0.6m/s,温度29-35℃,当发酵液中菌体浓度达到0.5亿个/mL时,结束固定化培养。
13.根据权利要求11所述的应用,其特征在于,所述的糖化液为糖蜜水解液、纤维素水解液、淀粉质水解液和合成培养基中的任意一种或两种的组合,总糖为200-260g/L;优选的糖化液为淀粉质水解液中的玉米糖化液。
14.根据权利要求11所述的应用,其特征在于,通过控制糖化液流速从而控制所述的管式反应器(1)中发酵残糖的总浓度为30-160g/L,优选120-160g/L。
15.根据权利要求11所述的应用,其特征在于,所述的间歇式发酵,是将经所述的管式反应器(1)反应后的糖化液,连续流加进入第一发酵罐中进行发酵反应,第一发酵罐中的发酵液加至60-85%v/v目标体积后,将经所述的管式反应器(1)反应后的糖化液,连续流加进入第二发酵罐中进行发酵反应,以此类推连续流加进入最后一个发酵罐;
其中,所述发酵罐中的发酵条件为30-37℃、50-300r/min,当单一发酵罐中的发酵残糖降至7-15g/L或还原糖降至1-3g/L时,该发酵罐发酵结束,流出发酵液并收集;
其中,通过控制流速和发酵罐体积以及发酵罐数量,使得最后一个发酵罐中发酵液加至60-85%v/v目标体积后,第一个发酵罐发酵恰好结束;将经所述的管式反应器(1)反应后的糖化液连续流加进入第一发酵罐中进行发酵反应,依次循环,实现间歇式发酵。
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