Method And System For A UHT Processing Of A Drinkable Plant-Based Food Product Under Sterile Conditions

1 . A method for UHT processing of a drinkable plant-based food product under sterile conditions,

in which the food product (RP; FP) in the form of a raw product (RP) used, a homogeneous mixture of a carrier liquid (TF) and at least one plantal substrate (TM), constitutes a continuous phase (TF+TM), and at least one solid admixture (B) is fed additively into the continuous phase (TF+TM), said admixture (B) constituting a dispersed phase (B) and, with the continuous phase (TF+TM), entering into a material solution in the form of the raw product (RP),

in which until a drinkable finished product (FP) is produced, the raw product (RP) is subjected, in the sequence mentioned in the following, to a thermal treatment (W) at least by a pre-warming (VW), a pre-heating (VE), a high-heating (HE), a heat-maintenance (HH) and a cooling (K), and in the course of the thermal treatment (W) undergoes a homogenization (HG), and

in which the thermal treatment (W) occurs in each case by indirect heat exchange between a product-side flow (RS) in the interior of a pipe and a heat carrier medium (Wm 1 , Wm 2 ) external to the pipe,

characterized in that

at least in one section of the thermal treatment (W), in which the at least one admixture (B) begins to precipitate out of the material solution, the raw product (RP), above a precipitation temperature (Ta),

on the one hand, a first pulsed flow (PS 1 ) is applied to the product-side flow (RS) in the interior of the pipe in the course of a pressure increase process using a pressure-increasing pump ( 9 ), said flow (PS 1 ) is superimposed on a second pulsed flow (PS 2 ) within the product side flow (RS) in the interior of the pipe resulting from the homogenization (HG) by means of a homogenizer ( 10 ), and

on the other hand, the product-side flow (RS) in the interior of the pipe is designed for a highly turbulent flow with a Reynolds number (Re) above 30,000 (Re>30,000).

2 . The method according to claim 1 ,

characterized in that

the Reynolds number (Re) is designed in a value range preferably between 35,000 and 80,000 (35,000≤Re≤80,000) and particularly preferably between 50,000 and 80,000 (50,000≤Re≤80,000).

3 . The method according to claim 1 ,

characterized in that

the required Reynolds number (Re) is ensured by an increased flow speed (c*) above 2.5 m/s in case of need (c*>2.5 m/s).

4 . The method according to claim 3 ,

characterized in that

the increased flow speed (c*) is designed in a range above 3.0 m/s (c*>3.0 m/s).

5 . The method according to claim 1 ,

characterized in that

first pulse maximums (x 1 ) relating to the volume flow of the first pulsed flow (PS 1 ) and second pulse maximums (x 2 ) relating to the volume flow of the second pulsed flow (PS 2 ) are different in size.

6 . The method according to claim 1 ,

characterized in that

the first pulse maximums (x 1 ) relating to the volume flow of the first pulsed flow (PS 1 ) have a first pulse frequency (f 1 ) and second pulse maximums (x 2 ) relating to the volume flow of the second pulsed flow have a second pulse frequency (f 2 ), and the first and the second pulse frequency (f 1 , f 2 ) are different in size.

7 . The method according to claim 1 ,

characterized in that

first pulse maximums (x 1 ) relating to the volume flow of the first pulsed flow (PS 1 ) and second pulse maximums (x 2 ) relating to the volume flow of the second pulsed flow (PS 2 ) are different in size, and

the first pulse maximums (x 1 ) relating to the volume flow of the first pulsed flow (PS 1 ) have a first pulse frequency (f 1 ) and second pulse maximums (x 2 ) relating to the volume flow of the second pulsed flow have a second pulse frequency (f 2 ), and the first and the second pulse frequency (f 1 , f 2 ) are different in size.

8 . The method according to claim 6 ,

characterized in that

the first pulse frequency (f 1 ) is smaller than the second pulse frequency (f 2 ).

9 . The method according to claim 6 ,

characterized in that

the first pulse frequency (f 1 ) has a 3 to 5 relationship to the second pulse frequency (f 2 ) (f 1 /f 2 =3/5).

10 . The method according to claim 1 ,

characterized in that

the precipitation temperature (Ta) is located above 110° C. in the high-heating (HE) and possibly already in the pre-heating (VE) and serves as a criterion for applying the features of claim 1 according to the invention.

11 . The method according to claim 1 ,

characterized in that

upon reaching

a prescribed pressure difference (Δp), relative to an initial pressure (p 9 ) at the outlet of the pressure increasing pump ( 9 ), and

a prescribed temperature difference (ΔT) between the raw product (RP) and a separate heat carrier medium (Wm 2 ) in the high-heating (HE), relative to an initial temperature difference (ΔTo),

the following steps (i) to (iv) are provided:

(i) first discharging (A 1 ) of the finished product (FP) from the UHT system ( 100 ) into a sterile tank arranged outside the UHT system ( 100 ) by means of water (FW);

(ii) second discharging (A 2 ) of a mixed phase of finished product (RP) and water (FW) into a gully circumventing the sterile tank by means of a subsequently defined quantity of water (FW);

(iii) circulating (Z) water (FW) within the UHT system ( 100 ) contaminated with raw and/or finished product (RP; FP) for a circulation time (Δt) that results from the complete elimination of the pressure difference (Δp) to the initial pressure (p 9 ) and of the temperature difference (ΔT) to the initial temperature difference (ΔTo), and

(iv) transitioning (UE) the UHT system ( 100 ) into renewed production readiness for a prepared batch-quantity of raw product (RP).

12 . The method according to claim 11 ,

characterized in that

in the course of the circulating (Z), the circulated volume flow of water (FW) is incrementally reduced by the pressure increasing pump ( 9 ) in conjunction with the homogenizer ( 10 ),

the decrease of the pressure difference (Δp) and of the temperature difference (ΔT) in this context is monitored and in each case maximum gradients are determined, and

the circulating (Z) is continued under the circulation conditions at the optimum of the determined maximums until the initial pressure (p 9 ) and the initial temperature difference (ΔTo) are reached.

13 . A UHT system for carrying out the method according to claim 1 for UHT processing of a drinkable plant-based food product under sterile conditions,

wherein the food product (RP;FP) in the form of a raw product (RP) used, a homogeneous mixture of a carrier liquid (TF) and at least one plantal substrate (TM), constitutes a continuous phase (TF+TM), and at least one solid admixture (B) is fed additively into the continuous phase (TF+TM), said admixture (B) constituting a dispersed phase (B) and, with the continuous phase (TF+TM), entering into a material solution in the form of the raw product (RP),

wherein the UHT system ( 100 ) is designed for thermal treatment (W) of the raw product (RP) with the objective of producing a drinkable finished product (FP) with, seen from the flow direction of the raw product, a pre-warming zone (VWZ) having at least one first ( 1 ) and if necessary a second heat exchanger ( 2 ) of the pre-warming zone, a pre-heating zone (VEZ) having at least one third heat exchanger ( 3 ) of the pre-heating zone, with a high-heating zone (HZ) having at least one heat exchanger ( 3 ) of the high-heating zone, with a heat-maintenance zone (HHZ) having at least one heat-maintainer ( 5 ), with a cooling zone (KZ) having at least one first heat exchanger ( 6 ) of the cooling zone and, if necessary, a second and a third heat exchanger ( 7 , 8 ) of the cooling zone, and in the course of the thermal treatment (W) with a homogenizer ( 10 ),

wherein the heat exchangers ( 1 - 4 ; 6 - 8 ) are designed in each case as shell-and-tube heat exchangers and are arranged in series connection, in which an indirect heat exchange occurs between the raw product (RP) which flows in multiple inner tubes ( 20 ) arranged in parallel and there constitutes a flow (RS) in the interior of a pipe, and a heat carrier medium (Wm 1 , Wm 2 ) that flows externally to the pipe around the inner tube ( 20 ),

characterized in that

a feed tank ( 11 ) is provided that is fluidically connected with the first heat exchanger ( 1 ) of the pre-warming zone via a supply line ( 13 ) in which a pumping apparatus ( 12 ) is arranged,

a supply line for water ( 14 ) flows into the supply line ( 13 ) upstream of the pumping apparatus ( 12 ),

the feed tank ( 11 ) is integrated in fluid communication into a circulation line system comprising the heat exchangers ( 1 - 4 ; 6 - 8 ) and the heat-maintainer ( 5 ) through to a sterile tank and a fifth line segment ( 13 . 5 ) that circumvents the sterile tank by bypass leading to the feed tank ( 11 ), and the supply line ( 13 ), and

a pressure increasing pump ( 9 ) is arranged downstream from the first heat exchanger ( 1 ) of the pre-warming zone and the homogenizer ( 10 ) is arranged downstream from the first heat exchanger ( 6 ) of the cooling zone.

14 . The UHT system according to claim 13 ,

characterized in that

in the flow-in section of the fifth line segment ( 13 . 5 ), an outflow line ( 15 ) to a gully opens out into the feed tank ( 11 ) from the fifth line segment ( 13 . 5 ).

15 . The UHT system according to claim 13 ,

characterized in that

the pressure increasing pump ( 9 ) is designed as a reciprocating pump with three single-acting pistons.

16 . The UHT system according to claim 13 ,

characterized in that

the homogenizer ( 10 ) is designed as a reciprocating pump with five single-acting pistons.

17 . The UHT system according to claim 13 ,

characterized in that

the pressure increasing pump ( 9 ) is designed for a counter pressure that ensures a Reynolds number (Re) of above 30,000, or an increased flow speed (c*) of above 2.5 m/s, and in that the product-exposed sections of the UHT system ( 100 ) between the pressure increasing pump ( 9 ) and the homogenizer ( 10 ) are designed for this counter pressure.

18 . The UHT system according to claim 13 ,

characterized in that

the inner tubes ( 20 ) of the shell-and-tube heat exchangers ( 1 - 4 ; 6 - 8 ) in each case have the features of the subject-matter of EP 1 567 818 B1.

19 . A drinkable plant-based food product such as almond milk consisting of the continuous phase (TF+TM), which consists of a homogeneous mixture of a carrier liquid (TF) and at least one plantal substrate (TM), wherein the plantal substrate (TM) is produced from almonds softened in a liquid provided for this purpose, such as water, then pressed or milled, and the plantal substrate (TM) is mixed into and homogeneously distributed in the carrier liquid (TF), such as water, with a dry substance content of 5 to 10%, and the dispersed phase (B), which consists at least of one solid admixture (B), with 1,800 to 2,000 mg calcium carbonate/liter of continuous phase, wherein the dispersed phase (B) with the continuous phase (TF+TM) enters into a material solution in the form of the raw product (RP), and produced through thermal treatment (W) in the UHT system according to claim 13 .