JP6219938B2 - プロバイオティックまたは他の微生物を含有する多孔性粉末製品の製造方法 - Google Patents
プロバイオティックまたは他の微生物を含有する多孔性粉末製品の製造方法 Download PDFInfo
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- JP6219938B2 JP6219938B2 JP2015516516A JP2015516516A JP6219938B2 JP 6219938 B2 JP6219938 B2 JP 6219938B2 JP 2015516516 A JP2015516516 A JP 2015516516A JP 2015516516 A JP2015516516 A JP 2015516516A JP 6219938 B2 JP6219938 B2 JP 6219938B2
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- A—HUMAN NECESSITIES
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- A23L—FOODS, FOODSTUFFS, OR NON-ALCOHOLIC BEVERAGES, NOT COVERED BY SUBCLASSES A21D OR A23B-A23J; THEIR PREPARATION OR TREATMENT, e.g. COOKING, MODIFICATION OF NUTRITIVE QUALITIES, PHYSICAL TREATMENT; PRESERVATION OF FOODS OR FOODSTUFFS, IN GENERAL
- A23L33/00—Modifying nutritive qualities of foods; Dietetic products; Preparation or treatment thereof
- A23L33/10—Modifying nutritive qualities of foods; Dietetic products; Preparation or treatment thereof using additives
- A23L33/135—Bacteria or derivatives thereof, e.g. probiotics
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- A—HUMAN NECESSITIES
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- C12N1/04—Preserving or maintaining viable microorganisms
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- A—HUMAN NECESSITIES
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Description
清澄化、遠心分離、または限外ろ過後に供される液体の微生物培養物;
凍結乾燥、真空乾燥、またはマイクロ波乾燥後に供される微生物培養物;および
貯蔵タンク、熱機械処理装置、表面熱交換器、攪拌/掻き混ぜ容器等内で増殖した微生物培養物。
ラクトバチルス・ヘルベティカスの細菌培養物(23kg/h(4%の全固形分(TS))、および全脂粉乳からなる担体(35kg/h(95%TS))をそれぞれポンプおよびホッパーを介して、450rpm、0.5MPa(5bar)の圧力かつ15℃で動作している二軸スクリュー押出機(TSE)に加え、59%TSの細菌培養濃縮物を形成した。二軸スクリュー押出機内で濃縮物を完全に混合および機械的に剪断してから通気装置に少なくとも1.3MPa(13bar)の圧力のCO2を注入して、安定した発泡体を形成した。その後発泡体を噴霧工程を介して乾燥チャンバに搬送し、そこで圧力をほぼ大気圧に減じて多孔性粉末を形成した。熱風を乾燥媒体として用いて粉末の水分を除去した。熱風の初期温度は入口温度が140〜150℃、出口温度が68℃であった。粉末の温度を測定したところ46℃であった。特に好ましい粉末の水分活性は0.15Awであり、得られる多孔性プロバイオティック粉末は4.3%の水分量を有するものである。
細菌(ラクトバチルス・ラムノサスGG、5%TS)ならびにタンパク質および炭水化物の混合物を含む担体組成物(再構成した全粉乳、95%TS)をそれぞれ24kg/hおよび30kg/hの速度で二軸スクリュー押出機に加えた。二つの成分を、320rpmのスクリュー速度、0.1MPa(10bar)の圧力、かつ20℃の温度の押出機中で混合、剪断し、55%の全固形分かつ粘度が約200mPa.sを超える培養濃縮物を形成した。次いで、1.3MPa(13bar)の圧力に加圧した二酸化炭素を濃縮物中に注入し、その結果得られた発泡体を、噴霧器を介して乾燥チャンバに搬送し、ここで乾燥チャンバ内を大気圧に減圧した。入口温度が140〜170℃で、出口温度が68℃の熱風を乾燥媒体として使用し、細菌を含有する多孔性粉末を形成した。
以下の6種のプロバイオティック試料の生存率を調べた。
・3種の液体試料:それぞれ、乾燥前のBb12、L.カゼイ、およびL.アシドフィルス(〜16%TS、MGより入手)
・3種の多孔乾燥試料:それぞれ粉末のBb12、L.カゼイ、およびL.アシドフィルス
(CFU/g)乾燥前=(CFU/ml)乾燥前/TS
次に、乾燥による生存率の低下を、以下の式を用いて計算した。
乾燥による生存率の低下=Log10(CFU/g)乾燥前-Log10(CFU/g)乾燥後
多孔乾燥したプロバイオティクスを90日間4℃で保存した後の生存率を表2に示す。90日間4℃で保存した後の粉末の対数減少値は0.40であった。
細菌の凍結ペレット(1011〜1012cfu/g)を40℃の水浴中で融解し、乳製品ベースのUHT濃縮物およびpH緩衝液(pH=6.2)とともに混合した。混合物の比率は1:1で、最終濃度の全固形分は18%である。3リットルの濃縮液を調製し、5Lのキャニスタに注ぐ。キャニスタを密閉したら、圧力が0.5MPaに達するまでCO2ガスを注入する。その後キャニスタを振とうして泡立てる。キャニスタは、出口ラインを介し乾燥チャンバ内の製品を噴霧するノズルに接続されている。乾燥粉末を回収し、さらに小さなベンチ流動床乾燥機で乾燥させ0.15の水分活性にする。次いで、粉末を窒素とともにアルミ袋に詰める。濃縮物および粉末の両方で生きている細胞を計数したところ、数値は8.1×1011cfu/gおよび3.2×1011cfu/gであった。生存率の対数減少値は0.40であった。
Claims (22)
- 少なくとも1種の液体微生物の培養物および担体組成物を含む液体濃縮物から微生物を含有する多孔性粉末製品の製造方法であって、担体組成物は少なくとも1種の炭水化物および少なくとも1種のタンパク質を含み、当該方法は以下の工程:
i)調製した後の液体濃縮物が5〜40℃の温度を有し、かつ当該温度において150mPa.sを超える粘度を有するように液体濃縮物を調製する工程;
ii)加圧した食品グレードのガスを0.3MPaを超える圧力で液体調製濃縮物に取り込む工程、ここで、工程ii)は、加圧したガスを液体濃縮物に注入して、その後、液体濃縮物と注入したガスを混合し0.6〜1.2kg/lの密度を有する安定した発泡体を形成することを含む;
iii)安定した発泡体を噴霧装置に搬送し、そこで安定した発泡体の圧力を0.3MPaから大気圧に減じ、ガスを安定した発泡体から放出させ、部分的に乾燥した製品を設ける工程;ならびに
iv)部分的に乾燥した製品を乾燥媒体に曝し、20℃で測定する場合の水分量を5%未満かつ水分活性を0.25Aw未満に下げて多孔性粉末製品を設ける、ここで工程(iv)における多孔性粉末製品の温度は50℃を超えない工程;を含む、微生物を含有する多孔性粉末製品の製造方法。 - 前記調製した液体濃縮物の温度が25〜35℃である、請求項1に記載の方法。
- 前記調製した液体濃縮物の温度が30℃である、請求項2に記載の方法。
- 前記安定した発泡体の密度が0.8〜1.1kg/lである、請求項1〜3のいずれか1項に記載の方法。
- 前記安定した発泡体の密度が0.85kg/lである、請求項4に記載の方法。
- 食品グレードのガスは、二酸化炭素、酸素、アルゴン、窒素、二酸化窒素、空気、またはそれらの混合物を含む群から選択される、請求項1〜5のいずれか1項に記載の方法。
- 液体濃縮物を泡立ちやすくそしてガスを溶解しやすくするために、担体組成物は、マルトデキストリン、ガラス転移温度が55℃を超える糖類、水溶性ゴム、グアーガム、又はキサンタン、ヒドロキシプロピルメチルセルロース(HPMC)、アルギネート、ペクチン、粉乳、炭水化物、またはタンパク質、あるいはそれらの混合物を含む、請求項1〜6のいずれか1項に記載の方法。
- 工程(iv)は、部分的に乾燥した製品を乾燥チャンバに吐出する第1サブ工程を含む、請求項1〜7のいずれか1項に記載の方法。
- 工程(iv)は、第1サブ工程の後に流動床上で実施する第2サブ工程を含む、請求項8に記載の方法。
- 工程(iv)において、20℃で測定する場合の部分的に乾燥した製品の水分活性を0.1超かつ0.25Aw 未満の値に下げる、請求項1〜9のいずれか1項に記載の方法。
- 工程(iv)において、20℃で測定する場合の部分的に乾燥した製品の水分活性を0.15Awに下げる、請求項10に記載の方法。
- 多孔性粉末製品のかさ密度が0.2g/cm3〜0.6g/cm3である、請求項1〜11のいずれか1項に記載の方法。
- 多孔性粉末製品のかさ密度が0.3g/cm3である、請求項12に記載の方法。
- 多孔性粉末製品は、30μm〜200μmの粒子サイズを有する自由流動性の粉末である、請求項1〜13のいずれか1項に記載の方法。
- 微生物は、細菌、酵母、真菌、およびプロバイオティクスを含む群から選択される、請求項1〜14のいずれか1項に記載の方法。
- 工程(ii)を、バッチ処理で動作する密閉タンク内で実施し、該工程(ii)において、前記ガスを、前記液体濃縮物を含む密閉タンク内に注入し、その後該密閉タンクを振とうして前記ガスと前記液体濃縮物を混合する、請求項1〜15のいずれか1項に記載の方法。
- 工程(ii)を、連続処理で動作する熱機械処理装置内で実施し、該工程(ii)において、前記ガスを該熱機械処理装置内に注入し、その後該熱機械処理装置内で前記液体濃縮物と混合する、請求項1〜15のいずれか1項に記載の方法。
- 熱機械処理装置は、単軸スクリュー押出機、二軸スクリュー押出機、ボテーター、およびスクレープ表面熱交換器を含む群から選択される、請求項17に記載の方法。
- 工程(i)も熱機械処理装置内で実施し、工程(i)および(ii)を連続的に実施するように構成する、請求項17または18のいずれかに記載の方法。
- 工程(ii)を、連続処理で動作する通気装置内で更に実施し、前記熱機械処理装置により混合した後の前記ガスと前記液体濃縮物を該通気装置内で更に混合する、請求項17〜19のいずれか1項に記載の方法。
- 工程(ii)を、連続処理で動作する通気装置内で更に実施し、該工程(ii)において、前記ガスを該通気装置内に注入し、その後該通気装置内で前記液体濃縮物と混合する、請求項1〜15のいずれか1項に記載の方法。
- 工程(iv)の後に凝集を行う、請求項1〜19のいずれか1項に記載の方法。
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FR2802212B1 (fr) | 1999-12-13 | 2002-03-01 | Agronomique Inst Nat Rech | Procede pour l'obtention d'une poudre contenant des micro-organismes viables, poudre obtenue selon ce procede et dispositif pour sa mise en oeuvre |
US20050266069A1 (en) * | 2002-09-06 | 2005-12-01 | Simmons Donald L | Stable probiotic microsphere compositions and their methods of preparation |
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DK2861086T3 (en) | 2017-05-01 |
WO2013185941A1 (en) | 2013-12-19 |
US20170280760A1 (en) | 2017-10-05 |
US20150150295A1 (en) | 2015-06-04 |
LT2861086T (lt) | 2017-06-26 |
PT2861086T (pt) | 2017-06-07 |
AU2013276851A1 (en) | 2015-01-22 |
AR091425A1 (es) | 2015-02-04 |
US9763472B2 (en) | 2017-09-19 |
EP2861086B1 (en) | 2017-03-22 |
ES2628897T3 (es) | 2017-08-04 |
JP2015519069A (ja) | 2015-07-09 |
EP2861086A1 (en) | 2015-04-22 |
SI2861086T1 (sl) | 2017-07-31 |
US10342248B2 (en) | 2019-07-09 |
NZ703071A (en) | 2016-09-30 |
HUE032531T2 (en) | 2017-09-28 |
PL2861086T3 (pl) | 2017-09-29 |
AU2013276851B2 (en) | 2016-12-08 |
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