JPH0488948A - Concentration of fancy drink such as coffee, teas - Google Patents
Concentration of fancy drink such as coffee, teasInfo
- Publication number
- JPH0488948A JPH0488948A JP20581090A JP20581090A JPH0488948A JP H0488948 A JPH0488948 A JP H0488948A JP 20581090 A JP20581090 A JP 20581090A JP 20581090 A JP20581090 A JP 20581090A JP H0488948 A JPH0488948 A JP H0488948A
- Authority
- JP
- Japan
- Prior art keywords
- reverse osmosis
- concentration
- concentrated
- drink
- coffee
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- 235000013616 tea Nutrition 0.000 title 1
- 238000001223 reverse osmosis Methods 0.000 claims abstract description 31
- 239000000796 flavoring agent Substances 0.000 claims abstract description 12
- 235000019634 flavors Nutrition 0.000 claims abstract description 12
- 238000002156 mixing Methods 0.000 claims abstract description 4
- 239000012528 membrane Substances 0.000 claims description 29
- 239000002131 composite material Substances 0.000 claims description 18
- 238000000034 method Methods 0.000 claims description 15
- 239000012466 permeate Substances 0.000 claims description 11
- 239000000284 extract Substances 0.000 claims description 10
- 239000007788 liquid Substances 0.000 claims description 10
- 235000013361 beverage Nutrition 0.000 claims description 9
- 241001122767 Theaceae Species 0.000 claims description 6
- 239000012141 concentrate Substances 0.000 claims description 6
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 abstract description 16
- 239000011780 sodium chloride Substances 0.000 abstract description 8
- 239000007864 aqueous solution Substances 0.000 abstract description 3
- 239000000243 solution Substances 0.000 abstract 5
- 239000000706 filtrate Substances 0.000 abstract 2
- 230000008569 process Effects 0.000 description 7
- 239000004952 Polyamide Substances 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- 229920002492 poly(sulfone) Polymers 0.000 description 4
- 229920002647 polyamide Polymers 0.000 description 4
- 239000004695 Polyether sulfone Substances 0.000 description 3
- 230000004907 flux Effects 0.000 description 3
- 229920006393 polyether sulfone Polymers 0.000 description 3
- 239000007787 solid Substances 0.000 description 3
- 230000000052 comparative effect Effects 0.000 description 2
- 238000007796 conventional method Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 238000000108 ultra-filtration Methods 0.000 description 2
- 239000004372 Polyvinyl alcohol Substances 0.000 description 1
- 108091006629 SLC13A2 Proteins 0.000 description 1
- 230000004075 alteration Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000009965 odorless effect Effects 0.000 description 1
- 230000003204 osmotic effect Effects 0.000 description 1
- 229920002451 polyvinyl alcohol Polymers 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000000717 retained effect Effects 0.000 description 1
- 238000004904 shortening Methods 0.000 description 1
- 230000009967 tasteless effect Effects 0.000 description 1
Landscapes
- Tea And Coffee (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明は、コーヒー、茶類等の嗜好飲料の濃縮方法に関
する。DETAILED DESCRIPTION OF THE INVENTION [Industrial Field of Application] The present invention relates to a method for concentrating a beverage of choice such as coffee or tea.
〔従来技術及び発明が解決しようとする課題〕コーヒー
、茶類等の嗜好飲料抽出液の濃縮法は、一般的には相変
化を伴う蒸発濃縮である。 このため重要なアロマ成分
が除去され、たとえ濃縮後アロマ成分を戻すとしても損
失と変質が生じる。[Prior Art and Problems to be Solved by the Invention] A method for concentrating extracts of favorite beverages such as coffee and tea is generally evaporation concentration accompanied by a phase change. This removes important aroma components, resulting in losses and alterations even if the aroma components are returned after concentration.
この品質的問題を解決するため、圧力を駆動力とする膜
性が検討され、膜性による２段処理か知られている（例
えば、特開昭５６−２９９５４号公報）。In order to solve this quality problem, a membrane process using pressure as a driving force has been studied, and a two-stage process using a membrane process is known (for example, Japanese Patent Laid-Open No. 56-29954).
しかしながらかかる方法では、第１段処理での可溶性固
型分を完全に保持できず、高濃度まで濃縮できない。
また後段においてはフレーバー成分の回収のみてなく、
低分子量の可溶性固型分も濃縮する必要があり、高負荷
となり膜寿命が短くなるという問題があった。However, in such a method, the soluble solid content in the first stage treatment cannot be completely retained and cannot be concentrated to a high concentration.
In addition, in the latter stage, not only the flavor components are recovered, but
It is also necessary to concentrate low-molecular-weight soluble solids, resulting in a high load and shortening the membrane life.
本発明はかかる問題点を解決するためになされたもので
あって、前段及び後段に特定の膜を用いて、特定操作圧
力で処理することにより、極めて効果的に目的とする濃
縮度を得ることがてきることを見い出して、本発明に至
ったものである。The present invention has been made to solve these problems, and it is possible to extremely effectively obtain the desired concentration by using specific membranes in the front and rear stages and processing at a specific operating pressure. The present invention was developed based on the discovery that this can be achieved.
即ち本発明は、コーヒー、茶類等の嗜好飲料抽出液の濃
縮方法において、
（ａＪ 嗜好飲料抽出液を、ルーズ逆浸透複合膜で５
０〜１２０ ｋｇｆ／ｃｍの操作圧力にて逆浸透処理し
、（ｂ） （ａ）工程から得た逆浸透透過液を、低圧
逆浸透複合膜で、３０〜５０ｋｇｆ／ｃｉの操作圧力に
て逆浸透処理し、濃縮液としてフレーバー成分を回収し
、（ｃ） （ａ）工程から得た濃縮液と（ｂ）工程か
ら得た濃縮液を混合して、目的の濃縮度を得ることを特
徴とするコーヒー、茶類等の嗜好飲料抽出液の濃縮方法
を提供する。That is, the present invention provides a method for concentrating a beverage extract such as coffee or tea, in which (aJ) a beverage extract is concentrated by a loose reverse osmosis composite membrane.
Reverse osmosis treatment is performed at an operating pressure of 0 to 120 kgf/cm, and (b) the reverse osmosis permeate obtained from step (a) is subjected to reverse osmosis treatment using a low-pressure reverse osmosis composite membrane at an operating pressure of 30 to 50 kgf/ci. The method is characterized by performing a permeation treatment, recovering flavor components as a concentrated liquid, and (c) mixing the concentrated liquid obtained from step (a) and the concentrated liquid obtained from step (b) to obtain the desired concentration. To provide a method for concentrating an extract of a favorite beverage such as coffee or tea.
本発明において（ａ）工程で用いるルーズ逆浸透複合膜
とは、０．１〜０．２％ＮａＣ１水溶液を圧力１０〜２
０ｋｇｆ／ａｔ、温度２５°Ｃで処理した時のＮａＣ１
阻止率が１０〜７０％、好ましくは１０〜３０％を示す
複合膜である。In the present invention, the loose reverse osmosis composite membrane used in step (a) refers to a 0.1 to 0.2% NaCl aqueous solution at a pressure of 10 to 2
NaC1 when processed at 0 kgf/at and temperature 25°C
The composite membrane exhibits a rejection rate of 10 to 70%, preferably 10 to 30%.
また（ｂｌ工程で用いる低圧逆浸透複合膜とは、０．１
〜０．２％ＮａＣ１水溶液を圧力ｌＯ〜１５ｋｇｆ／ｃ
ｄ、温度２５０Ｃて処理した時のＮａＣ１阻止率が９９
．０〜９９．９％を示す複合膜である。かかる複合膜の
活性層材質は、ポリアミド系、ポリビニルアルコール系
、スルホン化ポリエーテルスルホン系等が好ましく、特
に（ｂ）工程で用いる膜ではフレーバー成分の阻止性の
高いポリアミド系か望ましい。 またその支持層材質は
、特に限定されないか、例えば、ポリスルホン製、ポリ
エーテルスルホン製などの限外濾過膜等を挙げることか
できる。In addition, (the low pressure reverse osmosis composite membrane used in the BL process is 0.1
～0.2% NaCl aqueous solution at pressure lO～15kgf/c
d. NaCl rejection rate when treated at a temperature of 250C is 99
．． It is a composite membrane showing 0 to 99.9%. The active layer material of such a composite membrane is preferably a polyamide type, a polyvinyl alcohol type, a sulfonated polyether sulfone type, etc. In particular, for the membrane used in step (b), a polyamide type is preferable because it has a high ability to inhibit flavor components. The material of the support layer is not particularly limited, and examples thereof include ultrafiltration membranes made of polysulfone, polyethersulfone, and the like.
また上記複合膜を備えるモジュールの形態は特に限定さ
れないが、前段（ａ）に管状型、後段（ｂ）にスパイラ
ル型を用いるのか好ましい。Further, the form of the module provided with the composite membrane is not particularly limited, but it is preferable to use a tubular type for the first stage (a) and a spiral type for the second stage (b).
本発明においては、まず第１段目（（ａ）工程）として
嗜好飲料抽出液を、上記ルーズ逆浸透複合膜を用いて５
０〜１２０ｋｇｆ／ｃｄ、好ましくは１００〜１２０ｋ
ｇｆ／ｃｒｌの操作圧力、５〜１５°Ｃの処理温度にて
逆浸透処理し、３０〜５０Ｂｒｉｘまで濃縮する。 か
かるルーズ逆浸透複合膜を用いることにより、低分子量
の可溶性固型分をほとんど濃縮することができる。In the present invention, first, in the first stage (step (a)), the extract of the preferred beverage is extracted using the above-mentioned loose reverse osmosis composite membrane.
0-120kgf/cd, preferably 100-120k
Reverse osmosis treatment at an operating pressure of gf/crl and a processing temperature of 5-15°C and concentration to 30-50 Brix. By using such a loose reverse osmosis composite membrane, most of the low molecular weight soluble solids can be concentrated.
次いて第２段目（（ｂ）工程）として前工程（ａ）で得
られた逆浸透透過液を、上記低圧逆浸透複合膜て３０〜
５０ｋｇｆ／ｃｏ？、好ましくは３０〜４０ｋｇｆ／ｃ
ｆｆｌの操作圧力、５〜１５°Ｃの処理温度にて逆浸透
処理し、第１段目の透過液中のフレーバー成分を濃縮す
る。Next, in the second stage (step (b)), the reverse osmosis permeate obtained in the previous step (a) is passed through the low-pressure reverse osmosis composite membrane for 30 to 30 minutes.
50kgf/co? , preferably 30 to 40 kgf/c
The flavor components in the first stage permeate are concentrated by reverse osmosis treatment at an operating pressure of ffl and a treatment temperature of 5 to 15°C.
ここでは、フレーバー成分のみを濃縮することになるの
で、浸透圧は低く、比較的低圧により高濃度まで濃縮す
ることができる。Here, since only the flavor components are concentrated, the osmotic pressure is low, and it is possible to concentrate to a high concentration using relatively low pressure.
次いで、（ａｌ工程から得た濃縮液と（ｂ）工程から得
た濃縮液を混合することにより、目的の高濃縮度でかつ
フレーバー成分をほとんど保持した品質の良好な製品を
得ることができる。Next, by mixing the concentrated liquid obtained from the (al process) and the concentrated liquid obtained from the (b) process, it is possible to obtain a high-quality product that has the desired high concentration and retains most of the flavor components.
第１図は、本発明のフローの実例を示す説明図である。FIG. 1 is an explanatory diagram showing an example of the flow of the present invention.
本発明においては、濃縮倍率については、前段では糖度
３０〜４０°Ｂｒ１ｘまで濃縮可能であり、後段でも前
段の透過液中のフレーバー回収のため、高い容量減少率
、例えば３０〜４０倍まで容量減少可能で高濃度のフレ
ーバーが回収できる。 したかって、高濃縮度でかつフ
レーバー成分をほとんど保持した品質の良好な製品を得
ることができる。In the present invention, regarding the concentration ratio, in the first stage, it is possible to concentrate to a sugar content of 30 to 40°Br1x, and in the second stage, the volume can be reduced at a high rate of reduction, for example, 30 to 40 times, in order to recover the flavor in the permeate from the previous stage. possible and high concentration of flavor can be recovered. Therefore, it is possible to obtain a high-quality product that is highly concentrated and retains most of its flavor components.
以下に本発明の実施例を挙げるが、本発明はこれらに限
定されるものではない。Examples of the present invention are listed below, but the present invention is not limited thereto.
実施例
常法で得られた工業用コーヒー抽出液を、まずルーズ逆
浸透複合膜（Ｎａｉｌ阻止率＝１０％、膜面積＝１．６
ｄ、活性層＝スルホン化ポリエーテルスルホン系、支持
層＝ポリスルホン系）を備えた管状モジュールを用い、
操作圧力＝ １００ｋｇｆ／ｃｉ、線速＝ １．５ｍ／
ｓｅｅ、温度＝ｉｏ°Ｃの条件下にて濃縮を行った。１
．５Ｂｒｉｘを４０Ｂｒｉｘまで濃縮した時の平均Ｆｌ
ｕｘは１２．１／ｍ−ｈで、透過液の糖度は０．２Ｂｒ
ｉｘてあった。Example An industrial coffee extract obtained by a conventional method was first passed through a loose reverse osmosis composite membrane (Nail rejection rate = 10%, membrane area = 1.6
d, using a tubular module with active layer = sulfonated polyether sulfone system, support layer = polysulfone system),
Operating pressure = 100kgf/ci, linear speed = 1.5m/
Concentration was carried out under the conditions of 10°C and temperature = io°C. 1
．． Average Fl when 5Brix is concentrated to 40Brix
ux is 12.1/m-h, and the sugar content of the permeate is 0.2Br
There was ix.
ついで得られた透過液を、低圧逆浸透複合膜（ＮａＣ１
阻止率＝ ９９．５％、膜面積＝２ｍ、活性層＝ポリア
ミド系、支持層＝ポリスルホン系）を備えたスパイラル
型モジュールを用い、操作圧力＝３０ｋｇｆ／ａｌｒ、
線速＝０．２ ｍ／ｓｅｅ １温度＝１０℃の条件下に
て濃縮を行った。０．２Ｂｒｉｘを２ Ｂｒ１ｘまて濃
縮した時の平均Ｆｌｕｘは３５．２７／ｒＩｌ−ｈで、
透過液の糖度はＯＢｒ１ｘで、無味無臭であった。Next, the obtained permeate was passed through a low-pressure reverse osmosis composite membrane (NaCl
Rejection rate = 99.5%, membrane area = 2 m, active layer = polyamide type, support layer = polysulfone type) using a spiral type module, operating pressure = 30 kgf/alr,
Concentration was performed under the conditions of linear velocity = 0.2 m/see and temperature = 10°C. The average flux when 0.2Brix is concentrated by 2Br1x is 35.27/rIl-h,
The permeate had a sugar content of OBr1x and was tasteless and odorless.
また液量バランスは第２図のとおりであった。The liquid volume balance was as shown in Figure 2.
比較例
常法で得られた工業用コーヒー抽出液を、まず限外濾過
膜（概略分画分子量＝２，０００ ）を備えたチューブ
ラ−型モジュールを用い、操作圧力＝２０ｋｇｆ／ａｔ
、線速＝ １．５ｍ／ｓｅｅ、温度＝１０°Ｃの条件下
にて濃縮を行った。１．５Ｂｒｉｘを１５Ｂｒｉｘまで
濃縮した時の平均ＦｌｕＸは１６．４１／ｒｒＩ−ｈで
、透過液の糖度は１．３Ｂｒｉｘてあった。Comparative Example: An industrial coffee extract obtained by a conventional method was first processed using a tubular module equipped with an ultrafiltration membrane (approximate molecular weight cutoff = 2,000) at an operating pressure of 20 kgf/at.
Concentration was performed under the conditions of linear velocity = 1.5 m/see and temperature = 10°C. When 1.5Brix was concentrated to 15Brix, the average FluX was 16.41/rrI-h, and the sugar content of the permeate was 1.3Brix.
ついて得られた透過液を、高圧逆浸透複合膜（ＮａＣ１
阻止率＝９９％、膜面積＝２ゴ、活性層＝ポリアミド系
、支持層＝ポリスルホン系）を備えたスパイラル型モジ
ュールを用い、操作圧力＝ ７０ｋｇｆ／ｃｆｆｌ、線
速＝ ０．２ｍ／ｓｅｅ、温度＝１０℃の条件下にて濃
縮を行った。１．３Ｂｒｉｘを２５Ｂｒｉｘまて濃縮し
た時の平均Ｆｌｕｘは５．６１／−・ｈで、透過液の糖
度はＯＢｒ１ｘであった。The permeate obtained by this process was passed through a high-pressure reverse osmosis composite membrane (NaCl
Rejection rate = 99%, membrane area = 2 layers, active layer = polyamide type, support layer = polysulfone type) using a spiral type module, operating pressure = 70 kgf/cffl, linear velocity = 0.2 m/see, temperature Concentration was performed under the condition of =10°C. When 1.3Brix was concentrated to 25Brix, the average flux was 5.61/-·h, and the sugar content of the permeate was OBr1x.
また液量バランスは第３図のとおりであった。The liquid volume balance was as shown in Figure 3.
したがって、第２段目の逆浸透膜の負荷が高くなるとと
もに、混合された濃縮液のＢｒ１ｘも低い。Therefore, the load on the second-stage reverse osmosis membrane becomes high, and the Br1x of the mixed concentrate is also low.
第１図は本発明のフローの実例を示す説明図、第２図は
実施例における液量バランスを示す説明図、第３図は比
較例における液量バランスを示す説明図である。
１−・・・・−・−ルーズ逆浸透複合膜モジュール、２
・・・・低圧逆浸透複合膜モジュールFIG. 1 is an explanatory diagram showing an example of the flow of the present invention, FIG. 2 is an explanatory diagram showing a liquid volume balance in an example, and FIG. 3 is an explanatory diagram showing a liquid volume balance in a comparative example. 1-...--Loose reverse osmosis composite membrane module, 2
...Low pressure reverse osmosis composite membrane module
Claims (1)
おいて、 （ａ）嗜好飲料抽出液を、ルーズ逆浸透複合膜で５０〜
１２０ｋｇｆ／ｃｍ＾２の操作圧力にて逆浸透処理し、
（ｂ）（ａ）工程から得た逆浸透透過液を、低圧逆浸透
複合膜で、３０〜５０ｋｇｆ／ｃｍ＾２の操作圧力にて
逆浸透処理し、濃縮液としてフレーバー成分を回収し、
（ｃ）（ａ）工程から得た濃縮液と（ｂ）工程から得た
濃縮液を混合して、目的の濃縮度を得ることを特徴とす
るコーヒー、茶類等の嗜好飲料抽出液の濃縮方法。(1) In a method for concentrating an extract of a beverage of choice such as coffee or tea, (a) The extract of a beverage of choice is passed through a loose reverse osmosis composite membrane to
Reverse osmosis treatment is performed at an operating pressure of 120 kgf/cm^2,
(b) The reverse osmosis permeate obtained from step (a) is subjected to reverse osmosis treatment using a low-pressure reverse osmosis composite membrane at an operating pressure of 30 to 50 kgf/cm^2, and the flavor components are recovered as a concentrated liquid,
(c) Concentration of extracts of beverages such as coffee and tea, which is characterized by mixing the concentrate obtained from step (a) and the concentrate obtained from step (b) to obtain a desired degree of concentration. Method.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP20581090A JP2911975B2 (en) | 1990-08-01 | 1990-08-01 | Concentration method of favorite beverages such as coffee and tea |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP20581090A JP2911975B2 (en) | 1990-08-01 | 1990-08-01 | Concentration method of favorite beverages such as coffee and tea |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH0488948A true JPH0488948A (en) | 1992-03-23 |
| JP2911975B2 JP2911975B2 (en) | 1999-06-28 |
Family
ID=16513074
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP20581090A Expired - Lifetime JP2911975B2 (en) | 1990-08-01 | 1990-08-01 | Concentration method of favorite beverages such as coffee and tea |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP2911975B2 (en) |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5879733A (en) * | 1996-02-26 | 1999-03-09 | The Procter & Gamble Company | Green tea extract subjected to cation exchange treatment and nanofiltration to improve clarity and color |
| JP2003521880A (en) * | 1999-05-18 | 2003-07-22 | ソシエテ デ プロデユイ ネツスル ソシエテ アノニム | Stable coffee concentrate system |
| JP2007020441A (en) * | 2005-07-14 | 2007-02-01 | Ogawa & Co Ltd | Method for producing coffee beverage |
| US7875304B2 (en) | 1998-10-06 | 2011-01-25 | Xcafé LLC | Method of extracting a consumable material |
| US9480359B1 (en) | 2015-07-30 | 2016-11-01 | Meltz, LLC | Semi-continuous processes for creating an extract from coffee or other extractable materials |
| US11096518B2 (en) | 2015-03-20 | 2021-08-24 | Cometeer, Inc. | Systems for controlled heating and agitation for liquid food or beverage product creation |
| US11484041B2 (en) | 2017-04-27 | 2022-11-01 | Cometeer, Inc. | Method for centrifugal extraction and apparatus suitable for carrying out this method |
| US11724849B2 (en) | 2019-06-07 | 2023-08-15 | Cometeer, Inc. | Packaging and method for single serve beverage product |
-
1990
- 1990-08-01 JP JP20581090A patent/JP2911975B2/en not_active Expired - Lifetime
Cited By (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6063428A (en) * | 1996-02-26 | 2000-05-16 | The Procter & Gamble Company | Green tea extract subjected to cation exchange treatment and nanofiltration to improve clarity and color |
| US6268009B1 (en) | 1996-02-26 | 2001-07-31 | The Procter & Gamble Company | Green tea extract subjected to cation exchange treatment and nanofiltration to improve clarity and color |
| US5879733A (en) * | 1996-02-26 | 1999-03-09 | The Procter & Gamble Company | Green tea extract subjected to cation exchange treatment and nanofiltration to improve clarity and color |
| US7875304B2 (en) | 1998-10-06 | 2011-01-25 | Xcafé LLC | Method of extracting a consumable material |
| JP2003521880A (en) * | 1999-05-18 | 2003-07-22 | ソシエテ デ プロデユイ ネツスル ソシエテ アノニム | Stable coffee concentrate system |
| JP4562601B2 (en) * | 2005-07-14 | 2010-10-13 | 小川香料株式会社 | Method for producing coffee beverage |
| JP2007020441A (en) * | 2005-07-14 | 2007-02-01 | Ogawa & Co Ltd | Method for producing coffee beverage |
| US11096518B2 (en) | 2015-03-20 | 2021-08-24 | Cometeer, Inc. | Systems for controlled heating and agitation for liquid food or beverage product creation |
| US11751716B2 (en) | 2015-03-20 | 2023-09-12 | Cometeer, Inc. | Systems for controlled heating and agitation for liquid food or beverage product creation |
| US9480359B1 (en) | 2015-07-30 | 2016-11-01 | Meltz, LLC | Semi-continuous processes for creating an extract from coffee or other extractable materials |
| US9549635B1 (en) | 2015-07-30 | 2017-01-24 | Meltz, LLC | Semi-continuous apparatus for creating an extract from coffee or other extractable materials |
| US11484041B2 (en) | 2017-04-27 | 2022-11-01 | Cometeer, Inc. | Method for centrifugal extraction and apparatus suitable for carrying out this method |
| US11724849B2 (en) | 2019-06-07 | 2023-08-15 | Cometeer, Inc. | Packaging and method for single serve beverage product |
Also Published As
| Publication number | Publication date |
|---|---|
| JP2911975B2 (en) | 1999-06-28 |
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