WO2017064036A1

WO2017064036A1 - Method for obtaining energy from steam-containing vapor, and device for carrying out the method

Info

Publication number: WO2017064036A1
Application number: PCT/EP2016/074295
Authority: WO
Inventors: Rüdiger JANK; Stephen Schulte
Original assignee: Kuchenmeister Gmbh
Priority date: 2015-10-16
Filing date: 2016-10-11
Publication date: 2017-04-20
Also published as: DK3362741T3; PL3362741T3; DE102015220221A1; EP3362741B1; EP3362741A1

Abstract

The invention relates to a method for obtaining energy from steam-containing vapor, in particular baking vapor, in vapor-releasing systems, in particular baking systems. The dew point temperature τ of the steam-containing vapor is first increased to 95 to 99 °C, preferably 95 to 97 °C, the vapor is then condensed in at least one condensation chamber, and the vapor condensate obtained after the condensation of the vapor is used to obtain energy/heat. The invention likewise relates to devices for carrying out the method.

Description

Process for the production of energy from steam containing steam and apparatus for carrying out this process

The present invention relates to a method for generating energy from steam containing steam according to claim 1 and an apparatus for carrying out this method according to claims 14-16.

Description During the implementation of thermal processes, especially in food production, the atmosphere surrounding the food changes with regard to the enthalpy and composition of the substance mixture. By evaporation of water, the ambient air is enriched with water. The resulting air-vapor mixture, for example in the case of baking steam, usually has a dew point between 50 ° C and 90 ° C, preferably between 60 ° C and 80 ° C, depending on the relative humidity. The temperature of the exhaust air is between 80 ° C and 150 ° C, depending on the process heat. In addition to air and water vapor, the process air may contain, among other things, organic compounds, carbon, combustion gases, carbon dioxide and other substances. The resulting process air is called steam during baking and cooking processes. Accordingly, the baking in the baking chamber of the baking ovens in the baking chamber typically consist of water vapor, air and other organic constituents.

The baking steam is condensed after leaving the baking space, for example by using a suitable cooling medium such as water or condensate, which is conducted in a suitable condensation space in countercurrent to the baking steam (WO 2012/1 1 3800 A1). Depending on the dew point, the condensate temperature is between 60 ° C and 80 ° C. The resulting condensate can be removed via a heat exchanger, the heat energy, which is used for heating a medium, such as water, through the condensate located in the primary circuit. The temperature of the medium in the secondary circuit corresponds at most to the temperature of the condensate. The energy recovery is used here primarily the heating of service or drinking water. In industrial processes, on the other hand, enormous amounts of waste heat are sometimes generated in leakage currents, the full utilization of which far exceeds the required capacities, for example for hot water supply. For example, in the production of potato chips, heat losses of 5 MW / h are achieved. In addition, waste heat temperatures are required for specific technologies of heat utilization, which are usually above the normally occurring dew point of the vapor swaths.

It is therefore an object of the present invention to provide a method with which an improved utilization of the waste heat from swaths is effected and heat losses can be avoided.

This object is achieved by a method having the features of claim 1 and a device having the features of claims 14-16.

Accordingly, a method for energy recovery from steam containing steam, especially from baking steam, in steam-releasing systems, in particular baking systems (ovens) is provided. According to the method according to the invention, the dew point temperature τ of the steam containing the steam is first increased to 95 to 99 ° C, preferably 95 to 97 ° C. Subsequently, the steam is condensed in at least one condensation space and the condensation condensate obtained after condensation of the steam is used for energy recovery / heat recovery.

Accordingly, there is provided a method by which the dew point of the vapor swell can be increased to such an extent that the resulting swath condensate has waste heat temperatures which allow efficient use of the condensate even in the modern technologies of the absorption chiller and the ORC process the resulting condensate condensate after leaving the at least one condensation chamber has a temperature Τκ between 95 ° C and 99 ° C, preferably between 95 ° C and 97 ° C and thus far above the usual condensate temperatures of steam, in particular baking steam of 65 ° C. The dew point temperature or dew point is that temperature of a mixture of a gaseous and a liquid medium in which the condensation and the evaporation process of the wet component are in equilibrium. In this case, the gas is saturated with steam or there is a 100 percent saturation. In this equilibrium state, the vapor partial pressure is equal to the saturation vapor pressure of water.

The dew point temperature is essentially dependent on the water load X of the vapor swath, as well as the present pressure p. The relationship between these two parameters and the dew point temperature τ is described by the Magnus formula for describing the saturation vapor pressure of water.

Po, s = K, * exp - j (1)

For the constants of the Magnus formula, the temperature range Θ> 0 applies:

KL = 6.1078 / ιΡα K ₂ = 1 7.08085 K ₃ = 234.175 ° C

By transforming the equation X = R _tr , i_ / RD * PD, _S / p-P u, s to p _{D s} , the following formula is also obtained to describe the saturation vapor pressure of water:

Since the steam at the dew point is at saturation pressure, equations (1) and (2) can be equated and resolved according to the temperature Θ, giving the formula for describing the dew point temperature τ as a function of the water load X and the present pressure p.

From equation (3), it follows that a dew point temperature of 95 ° to 99 ° C. can be set correspondingly by varying the vapor pressure p as well as the water loading X.

Accordingly, various embodiments for increasing the dew point temperature result for the present method.

Thus, in a first embodiment, the steam containing the water vapor is compressed or compressed for the purpose of increasing the dew point temperature T.

Accordingly, the pressure level of the windrows is increased by compression of the moist air. The pressure required for the compression depends on the initial temperature of the windrow and the dew-point temperature to be achieved and is given by the following equation (4).

According to this variant of the present method, the steam contained in the steam is adjusted to a pressure p before the steam enters the condensation space

is compressed, so that a dew point temperature τ between 95 and 99 ° C, preferably 95 and 97 ° C is reached.

Based on the dew point curve for water vapor, a pressure is needed for the dew point increase, which seems uneconomical for energy recovery. However, by applying the Magnus formula and taking into account the moisture loading of the Schwadens, as well as the temperature-dependent constant, the above calculation algorithm according to equation (4) can be used with which the approximate effectiveness of the pressure increase can be calculated. Thus, with an increase in the dew point temperature from 65 ° C to 95 ° C, a pressure of about 250 kPa is required. If, on the other hand, the starting temperature of the windrows is selected to be 70 ° C, only a pressure of 100 kPa is required to increase the dew point to 95 ° C. Thus, a pressure increase of 150 kPa (1, 5 bar) leads to an increase in the dew point of 75 ° C to 95 ° C. Accordingly, this approach allows the selection of suitable swath conditions to ensure the economics of the process.

The application of the Magnus formula (which is typically based on approximate values at low temperature ranges) to the problem of increasing the dew point temperature of swaths that already have temperatures of over 60 ° C and more from the house by compressing thus allows an economical approach to energetically meaningful Use of the waste heat temperature contained in windrows.

The compression of the swath, e.g. the baking steam left the oven, before entering the steam into the condensation space using a compressor or compressor.

In a further embodiment of the present method, to increase the dew point temperature τ of the steam containing the steam, at least one liquid, in particular water or condensate, is sprayed into the steam before entering the condensation space. This increases the moisture content in the windrow.

In one embodiment of this process variant, the at least one liquid is atomized before entry into the swath. By atomizing the liquid is decomposed into droplets in the nanometer and micrometer range, in particular, the available surface of the liquid is increased.

This atomization of the liquid in the swaths can be done by ultrasonic atomization or by using piezo-controlled nozzles in the swaths. In the case of ultrasonic atomization, the liquid is atomized microscopically fine. In this case, the liquid medium is supplied with a pre-pressure of 1 -3 bar in the atomizer. The sonic gas (eg air or exhaust air) is excited to a vibration of 18 to 30 kHz. By the use of ultrasonic atomization, it is possible to reduce the energy expenditure for the evaporation. This reduces the necessary evaporation enthalpy and the condensate cools less. Ultrasonic atomization makes economic sense, especially at lower dew point differences; for example, at an entry dew point of the swaths above 75 ° C, preferably at 75 ° C to 85 ° C.

Another variant of the atomization represents the possibility of spraying water or condensate with piezo-driven nozzles or piezo-driven aerosol generators. In addition to the kinetic energy that is introduced by ultrasound or the piezoelectric element and reduces the droplet size or molecular clusters, a further energy enrichment by the application of a microwave voltage. This further breaks up molecular clusters and increases the rate of drying.

The change in the water load can be determined by the following equation (5), which is obtained by changing from equation (4):

From equation (5) it can be seen that increasing the water load X causes the dew point temperature to be increased. The goal is therefore to increase the water load, for example by spraying water into the moist air. Here, the condensate from the heat recovery can be used for spraying, with the result that the temperature of the sprayed water or condensate corresponds approximately to the dew point temperature of the moist air. In order to calculate the required amount of water to be sprayed, first the saturation vapor pressure p _{D s 2} ^after humidification is determined as a function of the dew point temperature τ _{2 of} the windrow to be achieved according to equation (6):

611 * exp (-1,91275 * 1 (Γ ⁴ + 7,258 * 1 (Γ ² * τ ₂ - 2,939

* 1 (Γ ⁴ * τ + 9,841 * 1 (Γ ⁷ *

- 1.92 * 1 (Γ ⁹ * τ |)

Using the saturation vapor pressure, it can now be calculated according to equation (7) which water loading X2 is necessary in order to achieve a dew point temperature τ ₂ in the moist air:

Due to the difference between the required water load X ₂ and the water load X ₁ before humidification, the required amount of water sprayed per kilogram of dry air can now be determined according to equation (8):

AX = X ₂ - x (8)

In order to obtain the absolute mass flow of the water to be injected rh _{+ w} , the difference of the water loadings is multiplied by the mass flow of the dry air according to equation (9):

m _{+ w} = AX * m _{tr L} (9)

Humidifying the steam with water causes the moist air stream to cool down considerably. This is due to the difference in temperature between the hot humid air and the sprayed water, especially the fact that the heat of evaporation of the water must be supplied by the humid air. For this reason, the energy accumulation or the energy input by spraying or atomizing the liquid such as water in the windrows, for example by means of ultrasound is necessary to counteract the loss of energy. The amount of liquid to be sprayed in the swath depends on the initial moisture content of the swath and is determined and controlled by the dew point temperature to be reached. The determination of the Ausgangsstaupunktes and the desired dew point can be done for example by means of suitable sensors and the amount of liquid to be sprayed is controlled by a corresponding nozzle.

In yet another variant of the present method, to increase the dew point temperature τ of the steam containing the steam, water vapor is introduced into the steam before entering the condensation space. By introducing water vapor into the windrows, a large amount of energy is supplied to the system, thereby greatly increasing heat recovery regardless of the mass flow of the dry air.

The production of the water vapor required for this purpose can be done in a large-scale water boiler, high-speed steam generators, clean steam generators, electrically heated steam generators or heat carrier heater.

In a particularly preferred variant, a forced-circulation boiler is used as a high-speed steam generator. Here, a continuous flow of water pipe coil is heated by a burner flame and the resulting flue gases in the countercurrent principle. Fuel and water are regulated so that wet steam with low residual water content is formed. With the help of a water separator it is possible to obtain saturated steam conditions. The advantage of using a forced-circulation boiler is the small footprint and the quick adaptation to load changes.

For humidification with saturated steam the same calculation basis applies as for humidification with water. The steps with the corresponding equations are identical. Instead of the mass flow of the water to be sprayed rh _{+ w} , the mass flow of the steam rh _{+ D to be introduced is} used. m _{+ D} = AX * m _{tr L}

The amount of steam to be introduced in the steam is also in this case dependent on the initial moisture of the windrow and is to be reached by the Dew point temperature determined and controlled. For example, by introducing 2.5 kwh / kg (dry) air, it is possible to increase the dew point temperature of a windrow by 20 ° C.

In a further embodiment of the present method, the condensation of the swaths with increased dew point temperature τ takes place by contacting the swaths in countercurrent with at least one cooling medium in the at least one condensation space.

As a cooling medium for wind condensation, water or steam condensate is preferably used, which is passed after cooling and passage through a heat exchanger back into the system.

In a preferred embodiment of the present method, the at least one cooling medium is at a flow rate between 0.5 m / min and 10 m / min, preferably between 1, 0 m / min and 5.0 m / min, more preferably between 1, 0 m / min and 2.5 m / min passed through the at least one condensation chamber. The cooling medium accordingly flows into the condensation space in the form of a liquid flow, in particular a continuous liquid flow. There is no spray condensation and thus no droplet formation of the incoming cooling medium in the condensation chamber. A spray condensation would not be feasible in the present process, since the swaths enter the condensation space with high flow velocity and thus the spray droplets instead of a filler to be entrained by the air flow, so that a reduced cleaning effect and a deteriorated energy utilization or worse Heat recovery occurs.

The cooling medium, such as water or steam condensate, can also be mixed with a suitable surface tension reducing additive. Suitable additives for this purpose are e.g. Surfactants or emulsifiers, which cause a better wetting of the ceramic surface.

Other additives, for example in the form of suitable acids can be used to adjust the pH of the cooling medium. In this case, an acidic pH of the cooling medium is preferred in order to prevent or limit the growth of microorganisms such as bacteria or fungi. The steam condensate obtained with the present process can be used as hot water via a heat exchanger, optionally after prior purification or filtration, in particular for the supply of hot water heating. In addition, the obtained Schwadenkondensat can be converted into at least one heat exchanger for heat recovery.

Accordingly, it is possible to use the obtained heat in-house or it is also possible to distribute the heat in the form of room heat or hot water by means of a district heating network of residential units or other facilities in the environment that require heat at a relatively low temperature level.

In a further variant, it is possible to use the obtained steam condensate for generating electricity in ORC (Organic Rankine Cycle) plants. ORC is a modern technology for using low temperature heat to generate electricity. Here, an organic medium is used, which evaporates at very low temperatures and drives a steam turbine or a generator for power production. The efficiency of the ORC process depends on the temperature level of the drive heat. It can efficiencies in the range of 10-25% can be realized, the efficiency increases with increasing drive temperature.

In addition to the abovementioned possibilities of using the windrow condensate, the resulting windrow condensate can be used for cooling in absorption refrigeration plants.

The present method is carried out in one of the following devices.

In a first variant, such a device comprises at least one horizontally and / or vertically arranged condensation space with at least one inlet for the entry of the steam containing steam and at least one outlet for the outlet of the condensed steam and at least one input for at least one cooling medium and at least one Output for the at least one cooling medium, wherein the respective inputs and outputs are arranged to each other such that steam and cooling medium flow through the condensation space in countercurrent, and at least one compressor for compressing the entering into the condensation space of water vapor contained swaths, wherein the at least one compressor along the supply line of the swaths upstream of the entrance for the entry of water vapor contained swaths is provided in the condensation space. In a second variant, such a device comprises at least one horizontally and / or vertically arranged condensation space with at least one inlet for the entry of steam containing steam and at least one outlet for the outlet of the condensed steam and at least one input for at least one cooling medium and at least one Output for the at least one cooling medium, wherein the respective inputs and outputs are arranged in such a way that swaths and cooling medium flow through the condensation space in countercurrent, and at least one device for spraying at least one liquid in the water vapor contained in the condensation chamber swaths, wherein the at least one device for spraying along the inlet of the swaths upstream of the inlet for the entry of steam containing steam is provided in the condensation space.

In yet another variant, such a device comprises at least one horizontally and / or vertically arranged condensation chamber with at least one inlet for the entry of the steam containing steam and at least one outlet for the outlet of the condensed steam and at least one input for at least one cooling medium and at least an outlet for the at least one cooling medium, wherein the respective inlets and outlets are arranged in such a way that steam and cooling medium flow through the condensation space in countercurrent, and at least one steam generator for introducing steam into the steam contained in the condensation space, wherein the at least a steam generator along the supply of the steam upstream of the entrance for the entry of water vapor contained steam is provided in the condensation space. In a preferred embodiment, the condensation of the swaths takes place on at least one surface of a condensing agent arranged in the condensation space. The at least one condensation agent is arranged in the condensation space such that it is at least temporarily contacted or moistened by the cooling medium. Due to this at least temporarily taking place wetting of the surface of the condensing agent with the coolant also eliminates the Necessity of washing the same, since possibly condensed or separated organic substances are dissolved directly in the swirl condensate. An essential aspect is that the surface of the condensing agent does not dry, otherwise there will be too difficult to remove encrustations on the surface of the condensing agent.

The at least one surface of the condensing agent arranged in the condensation space can have a cavity structure, in particular an open-cell system, a structured packing and / or an unstructured packing. It is also possible to provide or coat the condensing agents with organometallic or biocatalytic surfaces,

In a preferred embodiment, the open cell cell system used as condensing agent is in the form of a ceramic pore system with a pore size of 20 ppi, preferably 15 ppi, more preferably 10 ppi. For example, e.g. the use of ceramic foam with a corresponding pore size conceivable, this about 20% of the free cross-section of the condensation space, the e.g. is formed in the form of a column or a tube claimed.

It is further preferred if the at least one condensation space communicates with at least one heat exchange facility, through which the swirl condensate formed in the condensation space is guided.

The at least one condensation space may also be in communication with at least one ORC (Organic Rankine Cycle) installation in which the steam condensate formed in the condensation space is used to generate electricity.

Furthermore, there is the possibility that the at least one condensation space communicates with at least one apparatus for generating refrigeration in which the steam condensate formed in the condensation space is used for refrigeration.

The invention will be explained in more detail below with reference to the figures of exemplary embodiments. Show it:

Figure 1 is a schematic representation of an apparatus for performing the present method according to a first embodiment; Figure 2 is a schematic representation of an apparatus for carrying out the present method according to a second embodiment; and FIG. 3 shows a schematic illustration of an apparatus for carrying out the present method according to a third embodiment.

Exemplary embodiment 1: Humidification of the windrow with condensate FIG. 1 shows a schematic representation of the heat recovery by means of increasing the dew point temperature of the windrow by moistening the windrow with a liquid, in particular with a condensate.

Here emerging from a baking oven 1 baking steam or steam is introduced through a conduit 2 in a condensation chamber 3. Before the backwash enters the condensation chamber 3, liquid is sprayed into the baking swath using a suitable spraying device 4a, in particular by means of ultrasonic atomization.

The amount of liquid to be sprayed in the swath depends on the initial moisture content of the swath and is determined and controlled by the dew point temperature to be reached. Thus, the output dew point TP1 of the windrow before the spraying device 4a is determined. Depending on the initial dew point TP1 (e.g., 60 ° C) and the target dew point TP2 of the windrow detected after the spraying device, the amount of liquid to be fed by the spraying device 4a is regulated.

In the condensation chamber 3, the condensation of the moistened baking steam is carried out using a cooled condensate in countercurrent.

The condensate leaving the condensation chamber is fed to a heat exchanger 5 for heat recovery, Embodiment 2: Humidification of the windrow with saturated steam

Figure 2 shows a schematic representation of the heat recovery by increasing the dew point temperature of the windrow by wetting the wind with saturated steam.

Here emerging from a baking oven 1 baking steam or steam is introduced through a conduit 2 in a condensation chamber 3. Before the baking steam enters the condensation chamber 3, saturated steam is introduced into the baking steam. The necessary saturated steam is generated in a suitable steam generator 4b, in particular a high-speed steam generator.

The amount of saturated steam to be introduced into the windrows is also dependent on the initial moisture content of the windrow and is determined and controlled by the dew point temperature to be achieved.

Thus, the Ausgangstaupunkttemperatur TP1 of the windrow is determined before introducing the saturated steam. These initial values of a swath prior to the introduction of the saturated steam may be, for example, t = 98 ° C. rel.LF = 20% and TP1 = 60 ° C. at an absolute moisture Abs. F = 1 1 1 g / m ³ . The target values after introduction of the saturated steam are eg t = 98 ° C rel. LF = 100%, TP = 98 ° C with an abs. Humidity of 555g / m ³ .

Depending on the initial values and the target values of the windrow, the amount of saturated steam to be introduced in the windrows is regulated. In the condensation chamber 3, the condensation of the moistened baking steam is carried out using a cooled condensate in countercurrent.

The condensate leaving the condensation chamber is fed to a heat exchanger 5 for heat recovery,

Embodiment 3: Compression of the windrow

Figure 3 shows a schematic representation of the heat recovery by means of increasing the dew point temperature of the wind through compression of the windrow. Here emerging from a baking oven 1 baking steam or steam is introduced through a conduit 2 in a condensation chamber 3. Before the baking steam enters the condensation chamber 3, the baking steam is compressed. The pressure increase or compression of the baking steam is done using a suitable compressor or compressor 4c.

Again, the pressure increase is controlled by the output values and target values of the windrow. Thus, a pressure increase of 150 kPa (1, 5 bar) leads to an increase in the dew point of 75 ° C to 95 ° C.

Claims

claims

1 . Process for recovering energy from steam containing steam, in particular from baking steam, in plants releasing steam, in particular baking plants, characterized in that the dew point τ of the steam contained in the steam first to 95 ° C to 99 ° C, preferably 95 ° C to 97 ° C is increased, the swath is then condensed into at least one condensation space and the condensation condensate obtained after condensation of the swath is used for energy production and / or heat recovery.

2. The method according to claim 1, characterized in that to increase the dew point temperature τ of the steam contained in the steam, the swath is compressed or compressed.

3. The method according to claim 2, characterized in that the steam contained in the steam before entering the steam into the condensation space to a pressure p according to

4. The method according to claim 1, characterized in that to increase the dew point temperature T of the steam contained in the steam at least one liquid, in particular water or condensate is sprayed in the swaths before entering the condensation space.

5. The method according to claim 4, characterized in that the at least one

Liquid is atomized before entry into the swaths.

6. The method according to claim 4 or 5, characterized in that the liquid is introduced by means of ultrasonic atomization or using piezo-controlled nozzles in the swaths.

7. The method according to claim 1, characterized in that to increase the dew point temperature τ of the steam contained in the steam steam is introduced into the steam before entering the condensation space.

8. The method according to any one of the preceding claims, characterized in that the condensation of the swaths with increased dew point temperature τ takes place by contacting the swaths in countercurrent with at least one cooling medium in the at least one condensation space.

9. The method according to any one of the preceding claims, characterized in that the obtained Schwadenkondensat after exiting the at least one condensation space has a temperature Τκ between 95 ° C and 99 ° C, preferably 95 ° C and 97 ° C.

10. The method according to any one of the preceding claims, characterized in that the obtained Schwadenkondensat is used directly as hot water, in particular for the supply of hot water heaters.

1 1. A method according to any one of the preceding claims, characterized in that the resulting condensate condensate is transferred into at least one heat exchanger for heat recovery.

12. The method according to any one of the preceding claims, characterized in that the obtained Schwadenkondensat for power generation in ORC (Organic Rankine Cycle) systems is used.

13. The method according to any one of the preceding claims, characterized in that the obtained Schwadenkondensat is used for cooling in absorption refrigeration or compression refrigeration machines.

14. A device for carrying out a method according to claims 1 to 3, 8-13 comprising

at least one horizontally and / or vertically arranged condensation space having at least one inlet for the entry of the water vapor contained swaths and at least one outlet for the exit of the condensed swaths and at least one input for at least one cooling medium and at least one outlet for the at least one cooling medium, wherein the respective inputs and outputs are arranged relative to one another in such a way that the swaths and cooling medium flow countercurrently through the condensation space, and

at least one compressor for compressing the water vapor contained in the condensation chamber containing steam, wherein the at least one compressor is provided along the supply line of the windrows upstream of the entrance for the entry of water vapor contained swaths in the condensation space.

15. An apparatus for carrying out a method according to claims 1, 4-6 and 8-13 comprising

at least one device for spraying at least one liquid into the steam containing the steam entering the condensation space, the at least one device for spraying along the inlet of the steam upstream of the inlet for the entry of the steam

Steam containing steam is provided in the condensation space.

16. A device for carrying out a method according to claims 1, 7-13 comprising at least one horizontally and / or vertically arranged condensation space having at least one inlet for the entry of the water vapor contained swaths and at least one outlet for the exit of the condensed swaths and at least one input for at least one cooling medium and at least one outlet for the at least one cooling medium, wherein the respective inputs and outputs are arranged relative to one another in such a way that the swaths and cooling medium flow countercurrently through the condensation space, and

- At least one steam generator for introducing steam into the steam contained in the condensation chamber contained steam, wherein the at least one steam generator is provided along the supply line of the steam upstream of the entrance for the entry of water vapor contained steam in the condensation space.

17. The device according to one of claims 14 to 16, characterized in that the at least one condensation space is in communication with at least one heat exchange device, through which the swath condensate formed in the condensation space is guided.

18. Device according to one of claims 14 to 17, characterized in that the at least one condensation space with at least one ORC (Organic Rankine Cycle) plant is in communication, in which the swath condensate formed in the condensation space is used to generate electricity.

19. The device according to one of claims 14 to 18, characterized in that the at least one condensation space communicates with at least one device for cooling in conjunction, in which the swath condensate formed in the condensation space is used for cooling.