Cross-Reference to Related Applications

[0001] This application claims priority to U.S. Provisional Application No.

62/675,545, filed May 23, 2018, the disclosure of which is incorporated by reference herein in its entirety.

Technical Field

[0002] The present invention relates to concentration and/or dealcoholization systems and methods for fermented beverages or liquids.

Background Art

[0003] In U.S. Pat. No. 4,532,140, Bonnome discloses a method of manufacturing alcoholic beverage concentrates using multiple passes of membrane filtration, involving the combination of retentates from two passes. In U.S. Pat. No. 4,610,887, Galzy discloses a process for the concentration of small organic compounds below 200 in molecular weight using membranes capable of substantially retaining such compounds within the retentate. In U.S. Pat. No. 9,925,494, McGovern discloses methods for concentrating and retaining compounds of small molecular weight in multi-pass membrane systems with recycle loops.

Summary of the Embodiments

[0004] In accordance with one embodiment of the invention, a method for producing a beverage from a starting liquid having an ethanol component includes providing a first set of reverse osmosis pressure vessels, each pressure vessel having a feed inlet for a feed stream, a retentate outlet for a retentate stream, and a permeate outlet for a permeate stream, the first set having at least a first pressure vessel, a second pressure vessel and a third pressure vessel, the retentate outlet of the first pressure vessel fluidly coupled to the feed inlet of the second pressure vessel along a flow path, the retentate outlet of the second pressure vessel fluidly coupled to the feed inlet of the third pressure vessel, and the permeate outlet of the third pressure vessel fluidly coupled to the feed inlet of the second pressure vessel. The method further includes providing a pump coupled to the feed inlet of the first pressure vessel so that the starting liquid is pumped to the feed inlet of the first pressure vessel by the pump, blending the permeate stream of the third pressure vessel with the retentate stream of the first pressure vessel along the flow path to produce a blended stream having a pressure between about 850 psi to about 3000 psi, and obtaining the beverage from the retentate stream of the third pressure vessel.

[0005] In related embodiments, the pressure of the blended stream may be between about 1250 psi to about 3000 psi. The permeate stream of the second pressure vessel may be fluidly coupled to the feed inlet of the first pressure vessel. The method may further include providing a check valve, within the pump or between the pump and the feed inlet of the first pressure vessel, configured to prevent the starting liquid from going back through the pump. The method may further include providing a second pump coupled to the permeate outlet of the third pressure vessel so that the permeate stream of the third pressure vessel is pumped before blending with the retentate stream of the first pressure vessel. The method may further include providing a check valve, within the second pump or between the second pump and the feed inlet of the second pressure vessel, configured to prevent the permeate stream of the third pressure vessel from going back through the second pump. The method may further include providing a second set of reverse osmosis pressure vessels, each pressure vessel in the second set having a feed inlet for a feed stream, a retentate outlet for a retentate stream, and a permeate outlet for a permeate stream, the second set having at least a first pressure vessel and a second pressure vessel, the permeate outlet of the first pressure vessel in the first set fluidly coupled to the feed inlet of the first pressure vessel in the second set, the permeate outlet of the first pressure vessel in the second set fluidly coupled to the feed inlet of the second pressure vessel in the second set, the retentate outlet of the second pressure vessel in the second set fluidly coupled to the feed inlet of the first pressure vessel in the second set, the retentate outlet of the first pressure vessel in the second set fluidly coupled to the feed inlet of the first pressure vessel in the first set, providing a third pump coupled to the permeate outlet of the first pressure vessel in the first set, the feed inlet of the first pressure vessel in the second set, and the retentate outlet of the second pressure vessel in the second set, blending the permeate stream of the first pressure vessel in the first set with the retentate stream of the second pressure vessel in the second set to produce a second blended stream, and maintaining the permeate stream of the first pressure vessel in the second set at a pressure between about 300 psi to about 1,500 psi. In this case, the method may further include providing a check valve, within the third pump or between the third pump and the feed inlet of the first pressure vessel in the second set, configured to prevent the second blended stream from going back through the third pump. Each pressure vessel, in the first set of reverse osmosis pressure vessels, may have a hydrostatic burst pressure between about 2,400 psi to about 12,000 psi.

Brief Description of the Drawings

[0006] The foregoing features of embodiments will be more readily understood by reference to the following detailed description, taken with reference to the accompanying drawings, in which:

[0007] Fig. 1 depicts a continuous reverse osmosis system separated into stages where a second liquid is introduced at a mid-point in the system according to embodiments of the present invention.

[0008] Fig. 2 shows a continuous reverse osmosis system separated into stages where a second liquid is introduced at high pressure to a high pressure flow at a mid-point in the system according to embodiments of the present invention.

[0009] Fig. 3 shows a prior art continuous reverse osmosis system separated into stages where the permeate from the second stage is returned to the feed flow to the system.

[0010] Fig. 4 depicts a continuous reverse osmosis system separated into stages where the permeates from the second and third stage are returned to the feed flow to the system according to embodiments of the present invention.

[0011] Fig. 5 depicts a continuous reverse osmosis system separated into stages where the permeate from the second stage is returned to the feed flow to the system and the permeate from the third stage is introduced at high pressure to a high pressure flow between the first and second stages of the system according to embodiments of the present invention.

[0012] Fig. 6 depicts a continuous three-pass reverse osmosis system where the first pass is separated into stages, where the permeate from the second stage of the first pass is returned to the feed of the first pass, where the permeate from the third stage of the first pass is introduced at high pressure to a high pressure flow between the first and second stages of the system, where the permeate from the first stage of the first pass is introduced via high pressure pump to the feed inlet of the second pass, where the retentate of the second pass is returned to the feed inlet of the first pass, where the permeate of the second pass is introduced without a pump to the feed inlet of the third pass, and where the retentate of the third pass is returned to the feed inlet of the second pass according to embodiments of the present invention.

Detailed Description of Specific Embodiments

[0013] Definitions. As used in this description and the accompanying claims, the following terms shall have the meanings indicated, unless the context otherwise requires:

[0014] A“set” has at least one member.

[0015] The term“manifold” as used herein is a coupling between a flow line and a plurality of upstream or downstream flow paths, wherein for example, the plurality of flow paths may be associated with outlets of pressure vessels.

[0016]“Beverage” as used herein refers to any alcoholic beverage, including beer, wine, and cider, to any solution having alcohol (for example, an ethanol solution), and to any beverage made from fermented products, including beer, wine, cider, mead, and kombucha.

[0017]“Real Extract”, expressed as a percent weight, is defined as the mass of non ethanol and non-water compounds within a liquid or beverage.

[0018] Disclosed herein are multi-pass, multi-stage reverse osmosis systems for the concentration and/or dealcoholization of beverages (or other fermented liquids), including alcoholic beverages, that allow for boosted throughput or concentration factor. Systems described include multi-stage reverse osmosis systems that operate at low temperatures and high pressures, which are capable of reaching high beverage concentrations and are easily cleanable.

High Pressure Blending

[0019] Fig. 1 shows a reverse osmosis (RO) system having two pressure vessels or stages 100, 101 with a high pressure pump 102 that feeds a starting liquid or feed 105 into a feed inlet of the first stage 100. The first stage 100 produces a permeate 106 and a retentate

110 and the second stage 101 produces a permeate 107 and a retentate 108. The retentate 110 of the first stage 100 is fed into a feed inlet of the second stage 101. In addition, the system adds a feed 109 to an existing high pressure flow, in this example, retentate 110 from the first stage 100.

[0020] Fig. 2 shows a reverse osmosis system similar to Fig. 1 with an additional high pressure pump 203 adding the feed 109 into the retentate 110. A check valve 204, or other method of preventing backflow, is important for initialization of pump 203 when high pressure exists in the first stage 100, such that the pressure of feed 109 is equal to the pressure of retentate 110 plus the resistance of check valve 204 before feed 109 can flow into the second stage 101. In this manner, feed 109, which may be either substantially the same or different from feed 105, is added to the second stage 101 of the reverse osmosis process without requiring a depressurization and repressurization of retentate 110. The blended stream of retentate 110 and pumped feed 109 are coupled to the inlet of the second stage 101 in a series of reverse osmosis processes. In one embodiment of Fig. 2, feed 105 is a fermented beverage, and feed 109 is de-aerated water. In such an embodiment, the system allows for a specific method of bringing de-aerated water to high pressure so water may be blended in with the retentate 110 between two stages 100, 101 of the RO system. When a system, such as described in Fig. 2, was started without a check valve 204 (or back-flow prevention), the two pumps 102 and 203 must be started up simultaneously. Pumps 102, 203 may have different ramp speeds, and this can result in unexpected reverse flow through one pump if the other pump has ramped up first. The check valve 204 solves this problem as the check valve 204 allows the first pump 102 to be turned on, and then pump 203 to be turned on once pressure of retentate 110 is steady. In Fig. 2, the check valve 204 is shown as a separate component. However, in certain embodiments, the check-valve 204 may be built into the pump 203 or into pump 102 (in which case pump 102 is ramped up first). In yet another embodiment, a pump 102 or 203 may be employed that allows only for flow in one direction. Importantly, such a pump 102 or 203 should be able to withstand a back pressure of at least 600 psi when no power is provided to the pump 102 or 203.

[0021] Fig. 3 shows a prior art system with a two-stage reverse osmosis system designed for high overall retention. The system includes a pump 102 and a feed 105 that is supplied to a feed inlet of the first stage 100. The first stage 100 produces a permeate 106 and a retentate 110 and the second stage 101 produces a permeate 107 and a retentate 108. Retentate 110 is higher in concentration than feed 105, and retentate 110 of the first stage 100 is fed into a feed inlet of the second stage 101, where again a higher concentration retentate 108 is produced. Thus, permeate 107 will be of a higher concentration than permeate 106. For a high yield system, permeate 107 of the second stage 101 is returned to join with feed 105.

[0022] Fig. 4 shows a reverse osmosis system similar to Fig. 3 with a third stage 401 added. The third stage 401 of the reverse osmosis system is fed by retentate 108 of the second stage 101. The third stage 401 produces a permeate 402 and a retentate 403 . As permeate 107 is necessarily a higher concentration than permeate 106, so is permeate 402 a higher concentration than permeate 107. For a high yield system, both permeates 107 and 402 are returned to join with feed 105.

[0023] Fig. 5 shows a reverse osmosis system similar to Fig. 4, which is more efficient through the coupling of permeate 402 to the inlet of the second stage 101, where it blends with retentate 110 of the first stage 100 at high pressure. The reason for an efficiency gain is because the concentration of permeate 402 from the third stage 401 is higher than permeate 107 from the second stage 101 and, where permeate 107 may be close in concentration to feed 105, then permeate 402 may be close in concentration to retentate 110 of the first stage 100. In certain embodiments, the pressure at the blend point of the retentate 110 and the permeate 402 should be between 850 psi and 3000 psi, or more preferably 1250 psi to 3000 psi. Table 1 displays data demonstrating improved efficiency allowing for achievement of a higher factor of concentration over the same number of membranes when high pressure blending to a mid-point is employed. Here, again, high pressure pump 203 with a check valve 204 (or high pressure pump 102 with a check valve) allows for the mixing of two high pressure streams. Again, in other embodiments, a pump that does not allow for flow when the streams are not actively being pumped can alternatively serve as back-flow prevention in the place of pump 203 and check valve 204.

[0024] Table 1 : Concentration factors achieved on the same number of membranes when high pressure blending is and is not employed.

Table 1

[0025] Fig. 6 shows a reverse osmosis system similar to Fig. 5 with a three-stage, multi-pass system. The three stages are described in Fig. 5, including the pump 203 with check valve 204 to allow for high pressure introduction of permeate 402 from the third stage 401 to the retentate 110 of the first stage 100 in the system between the first stage 100 and the second stage 101. Additionally, permeate 106 of the first stage 100 is fed using pump 603 into a second set of pressure vessels configured into a two-pass system having a first pass

600 and a second pass 601. The permeate 606 of the first pass 600 is fed to the feed inlet of the second pass 601. Retentate 608, produced by the first pass 600, is kept within the system by returning the retentate 608 to join with feed 105 to be fed into the first stage 100. The second pass 601 produces a permeate 602, the final permeate output of the entire system in Fig. 6, and does so via backpressure formed by throttling the flow of retentate 604. By using backpressure to pressurize the second pass 601, the total number of pumps required in the system is reduced. To do this, the permeate 606 from the first pass 600 should be at a pressure between about 300 psi to about 1,500 psi. The concentration of retentate 608 and permeate 606 of the first pass 600, and permeate 602 and retentate 604 of the second pass

601 produced under a certain pressure formed by high pressure pump 603 alone will be equal to a system where the certain pressure is the sum of pressure supplied by high pressure pumps to each inlet. The high concentration retentate 604 of the second pass 601 is kept within the system by joining with permeate 106 from the first stage 100 and fed to the feed inlet of the first pass 600. The system is able to produce high concentration in retentate 403 of the third stage 401 and high overall retention with less energy than would otherwise be used if high pressure blending and backpressuring were not employed.

[0026] The embodiments of the present invention described above are intended to be merely exemplary; numerous variations and modifications will be apparent to those skilled in the art. All such variations and modifications are intended to be within the scope of the present invention as defined in the appended claims.