Device for condensing alcohol vapors from the heating of a water- and energy-saving boiler.

Abstract

Water and energy-saving alcohol vapor condensation device. The technical field of the present invention is that of alcohol distillation. In order to significantly reduce water consumption and consequently the energy required for cooling the heated water and to eliminate the discharge into the natural environment of copper-laden water, a device for condensing alcohol vapors 47 resulting from the heating of a boiler 10 containing a liquid to be distilled 23 consists of either a plate and gasket exchanger 50, or several plate and gasket exchangers mounted in series 51, 52, 53, 54 or a single stage exchanger equipped with cold water injection loops at each stage to control the stratification of the cooling layers and of which only the plate faces in contact with the distillate 48 are made of copper. The device is particularly suitable for the distillation of alcoholic liquids. Figure to be published for the abstract: [Fig 7]

Description

Title of the invention: Device for condensing alcohol vapors from the heating of a water- and energy-saving boiler.

[0001] Technical field: The technical field of the present invention is that of the distillation of alcohols.

[0002] State of the prior art: The distillation of spirits has existed since the Middle Ages. The tools and processes have gradually improved empirically over time to arrive at the so-called Charentais stills used today, among other places, in the Charentes region of France, Scotland and Ireland. All the stills used throughout the world to distill alcohols are entirely made of copper because this material is easy to form, an excellent heat conductor and, as demonstrated empirically over time, this material, in contact with the alcohol vapors during the flows, refluxes in the boiler and then during condensation in the coil, transforms and / or eliminates the sulfur and oil components that are undesirable from an organoleptic point of view.

[0003] As described in patent FR3117042A1 among others, the general principle of making a Charentais still is visible in [Fig.l] and comprises a boiler 10 configured to contain a liquid to be distilled 23, a gas burner 11 arranged under the boiler 10, a fire tower 12 integrated into the block 18 surrounding the boiler and configured to evacuate the burnt gases resulting from the combustion towards an evacuation conduit 13, a capital 14 surmounting the boiler 10 at the level of which condensation and reflux phenomena take place, a swan neck 15 collecting the alcohol vapors leaving the capital 14 and conveying them towards a coil 17 positioned in a refrigerating system composed of a condenser device 16 containing water 22 to condense the alcohol vapors which flow in liquid form 24 at the outlet of the coil 17 at the bottom of the condenser device 16 in the alcoholometer holder 20.The widely used device for preheating wines recovering calories around the pipework connecting the swan neck 15 to the condenser device 16 allowing the wines to be preheated to 45-50°C upstream of the boiler load is not shown.

[0004] The alcoholometer holder 20 illustrated in [Fig.2] is the receptacle for the liquid distillate 24 which allows the distiller to control and direct the destination of this flow of distillate 24 according to the Alcoholic Strength by Volume (ATV) of ethanol of the distillate 24 to the different tanks. The value indicated by the alcoholometer 26 floating in the liquid in the center of the alcoholometer holder 20 is corrected by the actual temperature of the distillate 24 read on the thermometer 27 using the Gay-Lussac tables to obtain the actual value of the TAV. The tap 25 at the bottom of the alcoholometer holder 20 is used to empty the latter at the end of the distillation cycle.

[0005] In simplified terms, for the production of Cognac brandy known as repasse distillation or double distillation or fractional distillation, the first pass distills wines containing 8 to 12% ethanol to produce a brouillis containing 28 to 32% ethanol. This brouillis distilled during the second pass will become a brandy with a TAV of around 70% ethanol.

[0006] It is the very significant difference in the latent heat of vaporization of ethanol (843 KJ / Kg at 78.3°C) with that of water (2,257 KJ / Kg at 100°C, therefore higher than this value at 78.3°C) which makes distillation particularly effective for distilling alcohols.

[0007] In simplified terms, the heating curve begins with heating at maximum intensity for 1h30 to 2 hours (depending on whether the wine preheated to 45°C or cold brouillis is being heated), then, when the first alcohol vapors pass through the swan neck, the heating intensity is reduced to 25% until the cut (brouillis tails at 8% TAV which will be mixed with the following wine batches, seconds at 30% TAV which will be mixed with the following brouillis batches and eau de vie tails at 8% TAV which will be mixed with the following wine or brouillis batches) to return to 100% heating intensity to finish extracting as much as possible the remaining ethanol present in the tails and the seconds which will be redistilled with the next batches of wine or brouillis according to the protocol followed.The vinasse remaining at the bottom of the boiler (65% of the initial wine charge, 45% of the initial brouillis charge) containing less than 2% ethanol is emptied to be cooled and treated.

[0008] Cutting is the term used to designate the action of changing the destination of the distillate from one container to another (Heads and tails, brouillis, eau de vie, seconds) according to its ethanol TAV, a change made just downstream of the alcoholometer holder.

[0009] The condenser device 16 is at the heart of the thermal control of the pouring temperatures of the distillate 24. This thermal control of the pouring temperatures of the brouillis (first heating), the heart, the seconds and the tails acts directly on the aromatic and taste characteristics of the eaux-de-vie. Thus, the major Cognac houses have defined specific pouring temperature ranges for each phase according to the quality and typicality sought for their eaux-de-vie.

[0010] For the wine heating (first heating), the pouring of the brouillis must be carried out at a temperature between 12 and 14°C measured at the alcoholometer holder 20. During this wine heating, the copper of the coil 17 interacts with the fatty acids to form soaps which become more or less insolubilized depending on the pouring temperature. These fatty acids are the precursors of numerous aromatic esters which contribute to the development of the aromas of eaux-de-vie. Fatty acids with long carbon chains produce rather detrimental fatty notes, while those with short carbon chains generate aromas that are particularly appreciated in Cognac eaux-de-vie. Pouring temperatures for brouillis above 14°C promote the passage of long-chain fatty acids, masking the aromatic typicity, while pouring temperatures below 12°C will lead to a reduction in short-chain fatty acids, which leads to an impoverishment of the aromatic structure.

[0011] For the heating of mash (second heating), the control of the pouring temperatures requires even more precision depending on the specific cooling requirements necessary for each fraction of distillate (heads, heart, seconds and tails). Generally speaking, the heads are poured between 17 and 19°C, the heart (eau de vie) around 18°C, the seconds and tails between 12 and 14°C.

[0012] The conduct of the thermal control of the condenser device 16 is therefore essential to be able to best improve the vapors of the aromatic compounds at the outlet of the swan neck 15 according to the desired typicality of the eaux-de-vie produced. The demonstrated and claimed advantage, for effectively both condensing and cooling, of the pipe 16 and coil 17 device, is due both to the large exchange capacity (length of the coil), to the thermal inertia conferred by the large volume of water contained in the pipe and to the capacity to maintain well-defined temperature strata from the water inlet to its outlet in the upper part of the pipe.

[0013] During the distillation of the brouillis (second heating), the cut between the heart and the seconds which involves changing the pouring temperature from 18°C ​​to 12°C must be anticipated in order to avoid having to inject too quickly a large quantity of cold water to compensate for the acceleration of the heating and the associated increase in flow rate. Too rapid an injection of a large quantity of cold water to evacuate part of the hot water in the upper part of the pipe would disrupt the temperature strata in the pipe. This de-stratification phenomenon greatly disrupts the distillation process at the level of the condensation of the alcohol vapors by giving samples described as poorly sorted by the tasters.

[0014] For a still used for first and second heatings, when the second heating of the brew follows a first heating of the wine, it is necessary to anticipate the preparation of the refrigerant by heating it gradually in order to be able to pour the heads and then the heart at around 18°C.

[0015] According to the same principles, another way of condensing alcohol vapors, very widely used for the iron production of Whisky is shown [Fig.3]. The alcohol vapors coming from the outlet of the swan neck 15 are conveyed to the top of a vertical tube and shell condenser 30. This condenser consists of a copper shell (or shell) 30 enclosing a bundle of copper tubes 31. The cooling water is injected into a tube 28 at the base of the condenser towards the inside of the tube bundle 31 to exit in the upper part through a tube 29. The alcohol vapors descend around the tubes 31 in the calender 30 and gradually condense to exit in the lower part towards the alcoholometer holder 20 in the form of liquid distillate 24.

[0016] As the underlying physics of the operation of all exchangers demonstrates, the inlet temperature of the refrigerant must be lower than the outlet temperature of the product to be cooled. In practice, and more specifically in the context of the distillation of alcohols, a water inlet temperature in the condensation device 2 to 3°C lower than the lowest pouring temperature of the distillate is the most widely implemented. Thus, the inlet temperature of the water in distilleries is in practice 8 to 10°C.

[0017] Problems related to cooling the distillate:

[0018] The Charentais still, whether for the production of Cognac with the pipe and coil device [Fig.l] or for the production of Whisky with the tube and calender device [Fig.3] is a large consumer of cooling water due to the need for a continuous supply throughout the distillation period.

[0019] On average, for a still with a capacity of 25 H1, the first heating (wine for Cognac or wash for Whisky) consumes 4 M3 of water and the second heating (scrambled wines for Cognac or low wines for Whisky) consumes 8 to 9 M3 of water. Water consumption is therefore around 35-40 liters of water per liter of pure alcohol produced to make Cognac or Whisky regardless of the capacity of the boiler.

[0020] Taking into account the volume of eaux-de-vie distilled annually in the AOC Cognac of approximately one million HectoLitres of Pure Alcohol (HLAP), the theoretical annual consumption of refrigeration water is therefore of the order of 4 million M3.

[0021] Although the water from the refrigeration process can return to the natural environment, the water law prohibits the discharge of this water at a temperature above 30°C, hence the need to use open passive systems (cooling slabs) or active systems (cooling circuits) to cool the water from 75-80°C to 30°C with an additional expenditure of energy for the second case.

[0022] Large distilleries, to reduce their water consumption, have opted for closed cooling circuits but with the additional constraint of having to cool the water from 75-80°C to 8-10°C to reinject it into the pipes at the cost of more complex systems and significant additional energy consumption to operate them continuously.

[0023] If the water supply to distilleries comes either from the drinking water network or from a spring, or from a catchment well, the fact remains that the consequences of global warming have an impact on the process. On the one hand, the reduction in precipitation and the level of groundwater makes the supply of catchment or drawing water more uncertain, on the other hand, mild winters result in a water supply (network or catchment) increasingly often at a temperature above 12°C which must therefore be partially cooled.

[0024] The same consequences of global warming and mild winters have an obvious impact on smaller distilleries using open cooling circuits before discharge into nature, which must invest in partial cooling units sized for their water consumption to comply with the water law.

[0025] Finally, a phenomenon not particularly recorded in the AOC Cognac but identified in whisky-producing regions, cooling water discharges into the natural environment are significantly loaded with copper, as demonstrated by numerous studies across the Channel, due to the very design of existing condensation systems circulating condensation / cooling water around or inside copper tubes, which is harmful to the environment.

[0026] Existing solutions:

[0027] The cooling solutions used by the largest distilleries allow for a reduction in net water consumption since they operate in a closed circuit.

[0028] Patent US2017312649A1 proposes recovering the energy available from the water leaving the condenser in the form of steam by means of a liquid / steam separator and one or more heat exchangers to use it to heat the boiler load and reinject the water thus cooled into the condensation system.

[0029] Patents FR3097037A1, FR3096901A1, EP3747522A1, FR3117042A1, FR3071851 describe a family of improved cooling devices with extraction of calories from the hot water of the condenser by means of various exchangers and / or heat pumps with the aim of using these recovered calories for heating the boiler and reinjecting the warm water at the base of the upper half of the condensation pipe modified with a separating wall in its middle, a wall crossed by the coil.

[0030] Additionally, patent FR3117042A1 describes a bypass system external to the condensation pipe connected to 3 sections of the coil, 2 directly above the separation wall and 1 directly below, allowing the temperature of the water in the upper part of the pipe to be adjusted to modulate the heat transfers between distillate and the upper and lower volume of water.

[0031] Patent FR2557990A1 describes the installation of various temperature and flow measurement probes associated with a control system making it possible to automate the control of the distillation phases by regulating the heating level of the boiler, the flow of cooling water in the condensation pipe and by controlling a multi-way solenoid valve making it possible to distribute the distillate to the containers corresponding to each phase of the distillation.

[0032] Criticism of the prior art:

[0033] Closed-circuit refrigeration water cooling solutions reduce water consumption by up to 90% but induce a continuous energy surcharge to operate the cooling unit potentially exceeding 200 KWH / HLAP. This additional energy cost should be compared to the energy consumption required for heating equivalent to 600-650 KWH / HLAP.

[0034] The impact of the solutions set out in the cited patents is not significant in terms of reducing the water consumption of the condensation system of a still and therefore concomitantly the energy consumption necessary for its cooling. In addition, some of these solutions prove to be complex to implement in terms of modification of existing equipment and difficult to control operationally for the distiller despite the probable implementation of an automatic control system.

[0035] Despite these various improvements, the water consumption required for the operation of distillation devices and the energy consumption required for cooling such volumes of hot water remain very high.

[0036] Furthermore, controlling condensation during casting phase changes, particularly during cuts, remains a delicate exercise to carry out due to the principle of thermal inertia conferred by a large volume of water used by these condensers (pipe and coil or tubes and calender). Statement of the invention

[0037] The present invention aims to remedy all or part of the drawbacks of the prior art.

[0038] The present invention relates to a device for condensing distillate vapors making it possible to divide the consumption of cooling water by up to a factor of 5 and to reduce by at least a similar factor the energy consumption necessary for cooling the hot water generated.

[0039] This device in all of its embodiments is also directly applicable to the manufacture of new stills.

[0040] Other features and advantages will appear in the detailed description which follows, examples of non-limiting embodiments of the invention illustrated by [Fig.4] to [Fig. 10] placed in the appendix and in which:

[0041] [Fig. 1] is a schematic representation of a distillation device illustrating an embodiment of the prior art.

[0042] [Fig.2] is a schematic representation of an alcohol meter holder used in a distillation device illustrating an embodiment of the prior art.

[0043] [Fig.3] is a schematic representation of another distillation device illustrating an embodiment of the prior art commonly used in the distillation of Whisky.

[0044] [Fig.4] is a schematic representation of a condensation device of the type plate and gasket exchanger used in the context of the present invention.

[0045] [Fig.5] is a schematic representation of the operating principle of a plate and gasket exchanger used in the context of the present invention.

[0046] [Fig.6] is a schematic representation of a distillation device implementing a plate and gasket exchanger used as a condensation device according to a first embodiment of the present invention.

[0047] [Fig.7] is a schematic representation of a distillation device using implements a plate and gasket exchanger group used as a condensation device according to a second embodiment of the present invention.

[0048] [Fig.8] is a schematic representation of how the plate and gasket exchangers of the condensing device illustrated in [Fig.7] are connected and operate according to the second embodiment of the present invention.

[0049] [Fig.9] is a schematic representation of a distillation device using implements a plate and gasket exchanger group used as a condensation device according to a third embodiment of the present invention.

[0050] [Fig. 10] is a schematic representation of how the plate and gasket exchangers of the condensing device illustrated in [Fig.9] are connected and operate according to the third embodiment of the present invention.

[0051] The following description of the invention is given without limitation, each characteristic of an embodiment being able to be combined with any other characteristic of any other embodiment or any other mode of use in an advantageous manner.

[0052] The general principle of the present invention is based, firstly, on the observation that in the general category of heat exchangers, plate and gasket exchangers are considerably more efficient than pipe and coil exchangers and tube and shell exchangers.

[0053] In terms of comparative performance, the plate and gasket exchanger is up to 5 times more energy efficient, takes up 4 to 5 times less floor space, is at least 10 times less expensive and, due to its disassembly, offers the possibility of carrying out maintenance, cleaning and component replacement operations quickly and easily, operations that are complex or even unthinkable with the other two systems.

[0054] Plate and gasket exchangers have also been widely adopted in the food industry in the broad sense, for example for milk pasteurization processes.

[0055] [Fig.4] illustrates a plate and gasket exchanger and [Fig.5] the operating principle between the plates.

[0056] As illustrated in [Fig.4], a plate exchanger is composed of several plates 40 and 41, mainly made of 316 or 316L stainless steel in the food industry. The plates are generally ribbed or fluted (chevrons) in shape. They are assembled by welding, brazing or compressed together in a frame 42 with gaskets 44 illustrated in [Fig.5] for plate and gasket exchangers.

[0057] The plates are generally thin (between 0.1mm and 0.8mm) and very closely spaced (between 5 and 10mm).

[0058] Between each plate, channels allow the parallel circulation of two fluids, one hot which is cooled from its inlet 32 ​​to its outlet 33 and the other cold which is heated from its inlet 36 to its outlet 35 in the device.

[0059] Thus, in a plate exchanger, one fluid circulates in the even-numbered pipes, while the other fluid circulates in the odd-numbered pipes. The transfer of heat energy takes place over the entire surface of the plates (heat transfer zone).

[0060] The chevron or channel construction of the plates allows the creation of a turbulence zone inside the exchanger, which facilitates heat exchanges and improves conductivity. As illustrated in [Fig.5], the chevrons of each contiguous plate are symmetrical in order to create the channels necessary for creating turbulence in the height of the exchanger.

[0061] Since the plate and gasket exchangers can be dismantled, it is also possible to add or remove plates to adapt their power to the installation or to a change of use.

[0062] The package composed of plates 40 and 41 and joints 44 is surrounded by a frame composed of two thick plates 42 and 43 connected by tie rods 39 to correctly compress the joints 44 and a guide rail 37 to position the even plates 40 and odd plates 41 during assembly.

[0063] Three different flow modes are possible depending on the applications:

[0064] A co-current circulation where the flow is parallel, the fluids converge in the same direction and the inlet of the two fluids is located on the same side of the exchanger.

[0065] A countercurrent circulation where the flow is parallel, but the fluids pass through the channels in opposite directions as illustrated in [Fig.5]. This is the best configuration to optimize the performance of a plate exchanger.

[0066] A cross-flow circulation where the flow is perpendicular between the two fluids and the inlet of each fluid is on each side of the exchanger and the respective outlets on the opposite face of the exchanger. This circulation configuration is called Z-shaped while the two previous ones are called U-shaped.

[0067] The present invention proposes to use as a device for condensing distillate vapors a single or, preferably, several plate and gasket exchangers mounted in series.

[0068] The preferred, but not exclusive, configuration of the plate and gasket exchangers of the present invention is a counter-current U-shaped circulation as illustrated in [Fig.5] with chevron plates whose half-angle beta with the vertical axis of the plate is of the order of 30°.

[0069] As demonstrated in the introductory remarks, the physicochemical interaction of the distillate in vapor phase then in liquid phase with the copper at the heart of the condensation device is essential for the good result desired from an organoleptic point of view. Thus, in the context of all the embodiments of the present invention, the distillate side face of each stainless steel plate of the exchanger, namely 41.2 and 40.2 illustrated in [Fig. 5] receives an electrolytic deposit of copper over its entire surface. The black arrows in [Fig. 5] represent the path of the distillate, the white arrows the path of the refrigeration liquid.

[0070] The distillate therefore condenses in channels made entirely of copper while the cooling water circulates in stainless steel channels. This configuration makes it possible to completely eliminate the release of copper into the natural environment for distilleries which use cooling water in an open circuit.

[0071] [Fig.6] illustrates a first embodiment of a distillation device equipped with a single condenser of the plate and gasket exchanger type with a U-shaped configuration. The distillate vapors 47 enter at the top of the front face of the exchanger 50 to exit in liquid form 48 at the alcohol meter holder 20. The cold refrigerant fluid, for example water, 45 enters the exchanger at the bottom of the rear face to exit hot at 46 in the upper part.

[0072] The refrigerant fluid inlet circuit in the exchanger comprises an instrumented injection circuit of the mixer type controlled by a control device. (not shown), injection circuit comprising for example a 3-way solenoid valve 62 coupled to a flow meter 66 and a temperature probe 62.2 on the exchanger side in order to regulate the flow rate and the injection temperature of the refrigerant fluid in relation to the needs linked to the flow rate and temperature setpoints fixed for the distillate 48 and as a function of the temperature of the cold refrigerant fluid 45 read on the probe 62.1 and the temperature of the hot refrigerant fluid 72 read on the probe 62.3 identical to the device illustrated [Fig.8].

[0073] The operating mode of this first embodiment is perfectly identical to the operating mode of a pipe and coil or tube and shell condenser, namely that it requires craftsmanship in that it is necessary to anticipate the cuts and the associated needs for increasing or decreasing the flow rates of cold refrigerant fluid depending on the variations in the flow rate of distillate. All of the elements such as the exchanger, the pipes and the various components constituting this embodiment can be partially or completely insulated.

[0074] The major improvement of this first embodiment is linked to the massive reduction in the volume of refrigerant fluid used thanks to the very large exchange surface between the distillate flow and the refrigerant fluid flow as well as to the turbulence created by the grooves.

[0075] According to a second illustrated embodiment [Fig.7], the condensation device comprises a series of 4 identical plate and gasket exchangers mounted in series. These exchangers are of the counter-current type (opposite distillate and water flows) in U (distillate and water inlets and outlets on the same face of the exchanger).

[0076] These 4 exchangers are fixed to a metal support structure 55 so that the outlet pipe from one exchanger to the inlet of the next exchanger is as straight and short as possible in order to avoid any stagnation / overpressure of the distillate flow whatever its physical state (vapor / liquid). The number of exchangers in this embodiment is at least 3 and is determined as a function, among other things, of the capacity of the boiler 10, the type of liquid to be distilled 23, the type of heating (first or second or both), the type of distillation (fractional, continuous or vacuum), the desired organoleptic qualities of the distillate 48.

[0077] The exchanger 51 is the first exchanger located at the top of the series of exchangers which receives at its upper inlet on the distillate side the alcohol vapors 47 coming from the boiler 10 and the capital 14 via the swan neck 15.

[0078] The partially condensed alcohol vapors 47.1 exit at the lower outlet of the exchanger 51 to enter directly into the upper inlet of the exchanger 52.

[0079] The condensate 47.2 exits at the lower outlet of the exchanger 52 to enter directly into the upper inlet of the exchanger 53.

[0080] The condensate 47.3 exits at the lower outlet of the exchanger 53 to enter directly into the upper inlet of the exchanger 54.

[0081] The distillate 48 exits at the lower outlet of the exchanger 54 to enter directly into the inlet pipe of the alcoholometer holder 20.

[0082] Following the reverse path, the refrigerant fluid 45 enters, at a temperature of 8-10°C for example, into the lower part of the exchanger 54 located at the bottom of the series of exchangers to exit at a higher temperature 45.1 in the upper part of the exchanger 54.

[0083] The refrigerant fluid 45.1 heated in the exchanger 54 is directed towards the lower inlet of the exchanger 53 to exit at a higher temperature 45.2 in the upper part of the exchanger 53.

[0084] The heated refrigerant fluid 45.2 is directed towards the lower inlet of the exchanger 52 to exit at a higher temperature 45.3 in the upper part of the exchanger 52.

[0085] The heated refrigerant fluid 45.3 is directed towards the lower inlet of the exchanger 51 to exit at a higher temperature 46 in the upper part of the exchanger 51 to be directed for example towards a storage tank 70 upstream of the refrigerant fluid refrigeration system (not shown).

[0086] The changes in the flow rate regime of the distillate 48 have a strong impact on the flow rate of refrigerant 45 required for cooling. This phenomenon is particularly significant during the core / second cut during the second heating. This cut occurs when the distillate TAV falls below the 60% mark where, concomitantly, the distillate temperature must fall from 18°C ​​for the core to 12°C for the seconds while the distillate outlet flow rate is multiplied by at least 2 (for example from 601 / min for the core to 1201 / min for the seconds) due to the strong increase in heating (times 2 to 3) required to compensate for the need to evaporate a distillate containing more and more water in proportion.

[0087] As described in

[0013] , a sudden injection of cold refrigerant fluid to deal with this change in regime is detrimental to maintaining good temperature stratification in the refrigerant fluid column of the condenser with harmful consequences on the quality of the distillate produced.

[0088] In order to avoid the traditional recommendation of anticipating by one hour this need for progressive injection of a large quantity of cold refrigerant fluid and the associated risks, the present invention in its second embodiment or in its third embodiment makes it possible to inject over a very short period (a few minutes at most) the quantity of cold refrigerant fluid just necessary for the change of regime without risking disturbing the necessary stratification of the temperatures of the refrigerant fluid.

[0089] [Fig.8] illustrates an exploded view of the second embodiment illustrated in [Fig.7] with the pipe connections as well as the various components necessary for its operation.

[0090] The path of the distillate from the vapor state 47 to the liquid state 48 is shown diagrammatically in continuous lines in each and between each exchanger. The path of the cold refrigerant fluid 45 to its hot outlet 46 is shown diagrammatically in dotted lines.

[0091] On the path of the alcohol vapors becoming distillate, each pipe connecting one exchanger to another is equipped with a temperature probe connected to the control device (not shown) with the probe 60.3 between the exchanger 51 and the exchanger 52, the probe 60.2 between the exchangers 52 and 53, the probe 60.1 between the exchangers 53 and 54 and finally the probe 60 between the exchanger 54 and the alcohol meter holder 20.

[0092] The refrigerant fluid inlet circuit in the exchanger comprises an instrumented injection circuit of the mixer type controlled by the control device (not shown). This refrigerant fluid supply circuit 45 (minimum pressure 2 bars, temperature for example 8-10°C) is equipped upstream with a valve 61 open at 100% during the distillation cycle and otherwise closed and with a connected temperature probe 62.1. Downstream of this valve, the cold refrigerant circuit is divided between a first branch towards the inlet of the exchanger 54 and a branch towards each connecting loop between the exchangers (branch 45.4 towards the connecting loop 49.1 between the exchangers 54 and 53, branch 45.5 towards the connecting loop 49.2 between the exchangers 53 and 52 and branch 45.6 towards the connecting loop 49.3 between the exchangers 52 and 51).

[0093] The branch towards the inlet of the exchanger 54 is equipped from upstream to downstream with a 3-way needle solenoid valve 62, a connected flow meter 66 and a connected temperature sensor 62.2. The third channel of the solenoid valve 62 is connected to the supply circuit of hot insulated refrigerant fluid 72 pressurized by the pump 71 and having a connected control temperature sensor 62.3 just upstream of the solenoid valve 62.

[0094] the connecting loops transferring the refrigerant fluid from one exchanger to the other are each instrumented and connected to a controlled injection loop of cold refrigerant fluid via the control device (not shown) to regulate the temperature gradient in each layer of refrigerant fluid in each exchanger according to the setpoints set as a function, among other things, and at a minimum, of the flow rate and the temperature of the distillate 48.

[0095] The refrigerant fluid connection loop 49.1 connecting the exchanger 54 to the exchanger 53 is equipped from upstream to downstream with a connected temperature probe 61.1, a calibrated non-return valve (for example at 0.5 bar) 65 and a connected bypass tee to the needle solenoid valve 69.1 on the second branch 45.4 of the cold refrigerant circuit.

[0096] The refrigerant fluid connection loop 49.2 connecting the exchanger 53 to the exchanger 52 is equipped from upstream to downstream with a connected temperature probe 61.2, a calibrated non-return valve (for example at 0.5 bar) 65.1 and a bypass tee connected to the needle solenoid valve 69.2 on the third branch 45.5 of the cold refrigerant fluid circuit.

[0097] The refrigerant fluid connection loop 49.3 connecting the exchanger 52 to the exchanger 51 is equipped from upstream to downstream with a connected temperature probe 61.3, a calibrated non-return valve (for example at 0.5 bar) 65.2 and a bypass tee connected to the needle solenoid valve 69.3 on the fourth branch 45.6 of the cold refrigerant fluid circuit.

[0098] The outlet of the hot refrigerant fluid exchanger 51 46 is equipped with a connected temperature probe 61.4 upstream of the thermally insulated storage tank 70.

[0099] All of the probes and solenoid valves are electrically connected to a control device (not shown) which automatically controls openings, closings and flow rates according to the actual flow rates and temperatures compared to the setpoints set for each usage cycle. All of the elements such as the exchangers, the pipes and the various components constituting this embodiment can be partially or completely insulated.

[0100] In stabilized operation, the solenoid valve 62 is open at X% on the cold refrigerant fluid path and closed on the hot refrigerant fluid path to allow a useful continuous flow rate of Dl / min depending on the actual temperature T°C of the cold refrigerant fluid 45 (for example between 8 and 10°C) and the desired distillate pouring temperature (12°C for the first heating mist, 12°C for the second and second heating tails).

[0101] For information purposes, when pouring the slurry (first heating) and the second and tails (second heating) at a temperature of, for example, 12°C at the probe 60 at the distillate outlet 48, the control temperatures on the refrigerant fluid circuit for an injected cold refrigerant fluid measured at 10°C on the probe 62.2 are at the probe 61.1 of the order of 23°C, at the probe 61.2 of the order of 40°C, at the probe 61.3 of the order of 58°C and 75°C at the probe 61.4.

[0102] Similarly, when pouring the second heating core at a temperature of, for example, 18°C ​​at probe 60 at the distillate outlet 48, the control temperatures on the refrigerant fluid circuit for an injected cold refrigerant fluid measured at 16°C on probe 62.2 are at probe 61.1 of the order of 28°C, at probe 61.2 of the order of 45°C, at probe 61.3 of the order of 62°C and 79°C at probe 61.4.

[0103] In the case of a second heating, at the end of this the temperature gradients in the series of exchangers are those listed as an example in paragraph

[0101] . For the following heating, upstream of the current supply (first alcohol vapors 47 arriving at the inlet of the exchanger 51), it is necessary to increase the temperature gradients to reach the configuration listed for example in paragraph

[0102] . This operation is carried out by the control device (not shown) using the 3-way solenoid valve 62 in mixing mode by partially injecting hot refrigerant fluid according to its actual temperature measured on the probe 62.3 in order to obtain an injection temperature measured on the probe 62.2 for example of 16°C.

[0104] The same operation is implemented when a still is used in mixed mode (same still used for the first and second heatings) when switching from a first heating to a second consecutive heating.

[0105] In the case of a second heating, when the seconds are cut, the necessary reduction in temperature of the refrigerant from the values ​​listed for example in paragraph

[0102] to the values ​​listed for example in paragraph

[0101] is carried out by the control device (not shown) by injecting cold refrigerant into each stage of the series of exchangers via the solenoid valves 62, 69.1, 69.2, 69.3 to reach the set temperatures read on the temperature probes 62.2, 61.1, 61.2, 61.3 and 61.4.

[0106] According to a third illustrated embodiment [Fig.9], the condensation device comprises a single exchanger 42.1 configured to be equivalent to a series of 4 identical plate and gasket exchangers mounted in series, materializing a series of four stages only on the refrigerant circulation channels of the exchanger. This exchanger is of the counter-current type (distillate and refrigerant flows opposite) in a U shape (distillate and refrigerant inlets and outlets on the same face of the exchanger). The number of stages of this embodiment is at least 3 and is determined as a function, among other things, of the capacity of the boiler 10, the type of liquid to be distilled 23, the type of heating (first or second or both), the type of distillation (fractional, continuous or vacuum), the desired organoleptic qualities of the distillate 48.

[0107] This third embodiment eliminates the need for intermediate inlets and outlets for the flow of distillate between the stages, the latter circulating from the upper inlet 47 of the alcohol vapors coming from the boiler 10 and the capital 14 via the swan neck 15 to the lower outlet 48 to enter directly into the inlet pipe of the alcohol meter holder 20 without discontinuity over the entire height of the exchanger 42.1.

[0108] As illustrated in [Fig. 10], the refrigerant fluid inlet circuit in the exchanger comprises an instrumented injection circuit of the mixer type controlled by the control device (not shown) identical to the second embodiment. The refrigerant fluid 45 at the set temperature set by the control command enters the lower part of the exchanger 42.1 to exit at a higher temperature at 45.1 in the upper part of the first stage of the exchanger 42.1.

[0109] The connecting loops transferring the refrigerant fluid from one exchanger to the other are each instrumented and connected to a controlled injection loop of cold refrigerant fluid via the control device (not shown) to regulate the temperature gradient in each layer of refrigerant fluid in the exchanger according to the setpoints set as a function, among other things, and at a minimum, of the flow rate and the temperature of the distillate 48.

[0110] As illustrated in [Fig.10], the outlet of the first stage 45.1 is connected to the inlet 46.1 of the second stage of the exchanger 42.1. This connecting loop is equipped from upstream to downstream with a connected temperature sensor 61.1, a calibrated non-return valve (for example at 0.5 bar) 65 connected to the 3-way needle solenoid valve 67.1 connected to the second branch 45.4 of the cold refrigerant circuit and a connected control temperature sensor 68.1 just before the inlet 46.1.

[0111] The refrigerant fluid entering at 46.1 heats up in its path through the second stage of the exchanger to exit at 45.2. The outlet of the second stage 45.2 is connected to the inlet 46.2 of the third stage of the exchanger 42.1. This connecting loop is equipped from upstream to downstream with a connected temperature sensor 61.2, a calibrated non-return valve (for example at 0.5 bar) 65.1 connected to the 3-way needle solenoid valve 67.2 connected to the third branch 45.5 of the cold refrigerant circuit and a connected control temperature sensor 68.2 just before the inlet 46.2.

[0112] The refrigerant fluid entering at 46.2 heats up in its path through the third stage of the exchanger to exit at 45.3. The outlet of the third stage 45.3 is connected to the inlet 46.3 of the fourth stage of the exchanger 42.1. This connecting loop is equipped from upstream to downstream with a connected temperature sensor 61.3, a calibrated non-return valve (for example at 0.5 bar) 65.2 connected to the 3-way needle solenoid valve 67.3 connected to the fourth branch 45.6 of the cold refrigerant circuit and a connected control temperature sensor 68.3 just before the inlet 46.3.

[0113] The refrigerant fluid entering at 46.3 heats up in its path through the fourth stage of the exchanger to exit at 46 to be directed for example towards a storage tank 70 upstream of the refrigerant fluid refrigeration system (not shown).

[0114] The hot refrigerant outlet 46 is equipped with a connected temperature probe 61.4 upstream of the thermally insulated storage tank 70.

[0115] All of the probes and solenoid valves are electrically connected to a control device (not shown) which automatically controls openings, closings and flow rates according to the actual flow rates and temperatures compared to the instructions set for each cycle of use. All elements such as exchangers, pipes and various components constituting this embodiment can be partially or completely insulated.

[0116] The operating modes of the second embodiment described from paragraph

[0100] to paragraph

[0105] are applicable identically to the third embodiment described above and illustrated in [Fig.9] and [Fig. 10].

[0117] The first advantage of the present invention is to potentially divide by up to a factor of 5 the consumption of refrigerant fluid necessary for each distillation cycle (first heating and second heating) conferred by the use of plate and gasket exchangers instead of pipe and coil or tube and shell type devices.

[0118] The second advantage of the present invention is to reduce by the same factor the consumption of electrical energy necessary for cooling the hot refrigerant fluid from the process due to the first advantage both for distilleries which operate in a closed circuit and for those operating in an open circuit since the volumes of refrigerant fluid used are smaller.

[0119] The third advantage of the present invention in its second embodiment or its third embodiment is to provide flexibility, speed and control of the fine control of changes in distillation regime over very short periods of the order of a few minutes at most, allowing an efficient and effective automated control mode via the control device during cuts and changes in heating (transition for the same still from a first heating to a second heating or vice versa) at a minimum without altering the organoleptic qualities of the distillate.

[0120] The fourth advantage of the present invention is to completely eliminate the presence of copper in the volumes of hot refrigerant fluid resulting from the distillation process for distilleries releasing these partially cooled volumes into the natural environment.

[0121] Those skilled in the art will easily understand the multiple possibilities offered by the present invention concerning both the number of exchangers in a series which will be at least 3 and preferably 4 but which could, among other things, depending on the types of products distilled, the distillation methods and the capacity of the boilers, be greater than 4, a feature which applies identically in the context of a single multi-stage exchanger on the refrigerant fluid side as described in the third embodiment.

[0122] Furthermore, still depending on the types of products distilled, the distillation methods and the size of the boilers among others, the exchangers of the same suite according to the second embodiment can be identical or different depending on the stage for example in terms of number of plates, configuration of the ribs / grooves of the plates in terms of depth, half-angle of inclination, shape, mode circulation (U-shaped, Z-shaped, co-current or counter-current), dimensions of each exchanger or type of exchanger such as semi-welded plates (welded distillate channels, refrigerant channel joints) or brazed plates.

[0123] Finally, those skilled in the art will appreciate that the technical characteristics of the present invention and the flexibility of its operating modes are directly and simply applicable to any device for distilling wines, beers, molasses or any other more or less alcoholic liquid, whatever the capacity of the container used for heating the distillation of these liquids, whether for fractional distillation in a still, continuous distillation in a column or for vacuum distillation.

Claims

Claims

1. Device for condensing alcohol vapors 47 from the heating of a boiler 10 containing a liquid to be distilled 23 consisting of a single plate and gasket exchanger 50 correctly dimensioned in terms of dimensions of the plates 40 and 41, number of plates 40 and 41, configuration of the ribs / grooves of the plates in terms of depth, half-angle of inclination when the ribs are chevrons 40.3, shape and size of the ribs / grooves, circulation mode (U-shaped, Z-shaped, co-current or counter-current) depending among other things on the capacity of the boiler 10, the type of liquid to be distilled 23, the desired organoleptic qualities of the distillate 48 in which the refrigerant fluid 45 is a heat transfer fluid.

2. Device for condensing alcohol vapors 47 from the heating of a boiler 10 containing a liquid to be distilled 23 consisting of a series of plate and gasket exchangers 51, 52, 53, 54 mounted in series correctly dimensioned in terms of dimensions of the plates 40 and 41, number of plates 40 and 41, configuration of the ribs / grooves of the plates in terms of depth, half-angle of inclination when the ribs are chevrons 40.3, shape and size of the ribs / grooves, circulation mode (U-shaped, Z-shaped, co-current or counter-current) depending among other things on the capacity of the boiler 10, the type of liquid to be distilled 23, the desired organoleptic qualities of the distillate 48 in which the refrigerant fluid 45 is a heat transfer fluid.

3. Device for condensing alcohol vapors 47 from the heating of a boiler 10 containing a liquid to be distilled 23 consisting of a single plate exchanger and gaskets 42.1 correctly dimensioned in terms of dimensions of the plates 40 and 41, number of plates 40 and 41, configuration of the ribs / grooves of the plates in terms of depth, half-angle of inclination when the ribs are chevrons 40.3, shape and size of the ribs / grooves, circulation mode (U-shaped, Z-shaped, co-current or counter-current) depending among other things on the capacity of the boiler 10, the type of liquid to be distilled 23, the desired organoleptic qualities of the distillate 48 in which the refrigerant 45 is a heat transfer fluid and in which the joints of the plates only on the refrigerant side are organized to form a series of stages with the corresponding inlets-outlets of the refrigerant from one stage to the next.

4. Condensing device according to claims 1 or 2 or 3 characterized in that the refrigerant inlet circuit in the exchanger comprises an instrumented injection circuit of the mixer type controlled by a control device, injection circuit comprising for example a 3-way solenoid valve 62 coupled to a flow meter 66 and a temperature probe 62.2 on the exchanger side in order to regulate the flow rate and the injection temperature of the refrigerant in relation to the needs linked to the flow rate and temperature setpoints fixed for the distillate 48 and as a function of the temperature of the cold refrigerant 45 read on the probe 62.1 and the temperature of the hot refrigerant 72 read on the probe 62.

3.

5. Condensing device according to claim 2 characterized in that the connecting loops transferring the refrigerant fluid from one exchanger to the other are each instrumented and connected to a controlled injection loop of cold refrigerant fluid via a control device to regulate the temperature gradient in each layer of refrigerant fluid in each exchanger according to the setpoints fixed as a function, among other things, and at a minimum, of the flow rate and the temperature of the distillate 48.

6. Condensing device according to claim 3 characterized in that the connecting loops transferring the refrigerant fluid from one stage of the exchanger to the other are each instrumented and connected to a controlled injection loop of cold refrigerant fluid via a control device to regulate the temperature gradient in each layer of refrigerant fluid in each stage of the exchanger according to the setpoints fixed as a function, among other things, and at a minimum, of the flow rate and the temperature of the distillate 48.

7. Condensing device according to claims 2 or 3 characterized in that the number of exchangers mounted in series or the number of stages on the refrigerant side of a single exchanger are at least 3 and depend among other things on the capacity of the boiler 10, the type of liquid to be distilled 23, the type of heating (first or second or both), the type of distillation (fractional, continuous or vacuum) and the desired organoleptic qualities of the distillate

8. HO. Condensing device according to claims 1 or 2 or 3 or 7 characterized in that the distillate side face of each stainless steel plate of each exchanger, namely 41.2 for plates 41 and 40.2 for plates 40, receives an electrolytic deposit of copper over its entire surface.

9. Condensing device according to claims 1 or 2 or 3 or 7 or 8 characterized in that the exchangers are semi-welded plate exchangers or brazed plate exchangers.

10. Condensing device according to any one of the preceding claims, characterized in that the exchangers and, where appropriate, the pipes comprising the refrigerant fluid inlet circuit, the connecting loops, the branches of the refrigeration circuit and the hot water circuit are insulated.

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