EP3707306B1 - Machine de production ou de traitement d'une bande de matière fibreuse et procédé de recyclage de vapeur d'un utilisateur de vapeur dans la machine - Google Patents

Machine de production ou de traitement d'une bande de matière fibreuse et procédé de recyclage de vapeur d'un utilisateur de vapeur dans la machine Download PDF

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Publication number
EP3707306B1
EP3707306B1 EP18803556.2A EP18803556A EP3707306B1 EP 3707306 B1 EP3707306 B1 EP 3707306B1 EP 18803556 A EP18803556 A EP 18803556A EP 3707306 B1 EP3707306 B1 EP 3707306B1
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EP
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Prior art keywords
steam
pressure level
condensate
pressure
barg
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EP18803556.2A
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German (de)
English (en)
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EP3707306A1 (fr
Inventor
Martin Dauner
Thomas Mack
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Voith Patent GmbH
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Voith Patent GmbH
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    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21F—PAPER-MAKING MACHINES; METHODS OF PRODUCING PAPER THEREON
    • D21F5/00—Dryer section of machines for making continuous webs of paper
    • D21F5/20—Waste heat recovery
    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21F—PAPER-MAKING MACHINES; METHODS OF PRODUCING PAPER THEREON
    • D21F5/00—Dryer section of machines for making continuous webs of paper
    • D21F5/18—Drying webs by hot air
    • D21F5/181—Drying webs by hot air on Yankee cylinder

Definitions

  • the invention relates to a machine for producing or processing a fibrous web according to claim 1, as well as a method for steam recovery according to claim 10.
  • a hot air hood is used on the Yankee cylinder to dry the web.
  • the hot exhaust air from this hood is usually used again to generate steam.
  • Various methods for this purpose are known from the prior art.
  • the EP 3 150 761 suggests a solution that can do without this vapor collection tank. In this solution, however, components are required to generate the motive steam by recovering waste heat, which can withstand comparatively high pressures and are therefore usually expensive and maintenance-intensive.
  • Another object of the invention is to reduce the investment costs.
  • the steam consumer is designed as a steam-heated cylinder, in particular as a Yankee cylinder.
  • the invention is not limited to this.
  • Other steam consumers such as, for example, steam blower boxes, air conditioning devices or the like, are also conceivable.
  • This machine according to the invention has the essential advantage over the prior art that the pressure level of the steam supply can be optimally adapted independently of the pressure level of the live steam network of the system. Since the live steam network of the system supplies one or more other steam consumers in addition to the steam consumer of the device according to the invention, e.g. in addition to the Yankee cylinder, the pressure in this live steam network will be selected so high that all connected consumers can be adequately supplied with it. However, this first pressure level is usually higher than the pressure level that is necessary to supply the steam consumer and / or possible further units in the device according to the invention. In addition, the device according to the invention manages without an additional steam collecting container for the generated steam.
  • thermocompressor can be operated with motive steam at a high pressure level. This is beneficial for the efficiency of the compressor and leads to lower investment costs.
  • the motive steam for the thermocompressor can be taken directly from the live steam network.
  • the pressure level of this live steam network is often more than 5 barg, in particular more than 8 barg or 15 barg higher than the second pressure level. Therefore the live steam network is very suitable as a source for the motive steam.
  • the second pressure level can be 0.5 bar to 5.0 bar higher than the setpoint pressure with which the steam is introduced into the steam consumer.
  • the thermocompressor can be used to generate steam at a low pressure level - in particular expansion steam, which is created by expanding the condensate removed from the steam consumer and / or through-flow steam, which is required for dewatering the Yankee, or a mixture thereof - by means of the To compress motive steam to the pressure level with which the steam is introduced into the steam consumer (target pressure of the steam consumer).
  • target pressure of the steam consumer.
  • steam with a target pressure between 3.0 barg and 9.0 barg is used in the steam consumer.
  • the target pressure can, however, also be lower, for example 1.5 barg or higher, for example 10.0 barg.
  • the pressure level with which the steam is introduced into the steam consumer corresponds to the second pressure level.
  • this setpoint pressure is below the second pressure level.
  • the pressure can be reduced from the second pressure level to the target pressure via a heating and / or supplementary valve before it is introduced into the steam consumer.
  • the steam consumer can also be supplied with steam, which arises, for example, as expansion steam in a first separator, the pressure of this steam being raised to the target pressure of the steam consumer by means of the thermocompressor.
  • the second pressure level in the steam supply, which can be selected independently of the first pressure level and which can be adjusted specifically to the requirements of the steam consumer.
  • the second pressure level will be significantly lower than the first pressure level.
  • the second pressure level is advantageously between 2 bar and 10 bar below the first pressure level, preferably between 4 bar and 9 bar below the first pressure level.
  • the steam generating device comprises, in addition to a heat exchanger, at least one throttle element to which To at least partially evaporate condensate after passing through the at least one heat exchanger, as well as a separator to which the at least partially evaporated condensate can be fed and to which the return line can be connected.
  • the at least partial evaporation of the condensate does not take place directly in the heat exchanger.
  • Such direct evaporation can lead to the formation of deposits in the heat exchanger, which in turn can lead to a reduction in performance or to damage to the heat exchanger.
  • the outlay for feed water treatment or condensate treatment can also be higher.
  • the throttle element can advantageously be a fitting, a diaphragm or a similar device which is suitable for at least partially evaporating the condensate after it has passed through the heat exchanger.
  • the condensate is evaporated directly at the inlet of the separator or in the interior of the separator.
  • the separator has the function of an expansion tank.
  • the separator and the throttle element form a functional unit.
  • the steam supply can be decoupled from the live steam network in advantageous embodiments by means of a valve, in particular a regulating or throttle valve or a throttle element.
  • a valve in particular a regulating or throttle valve or a throttle element.
  • the invention is not limited to these embodiments.
  • the connectivity of the two steam systems is advantageous. On the one hand, this can be used for the initial filling of the steam supply and the steam consumer, etc.
  • the steam is reduced from the first pressure level of the live steam network to the second pressure level of the steam supply.
  • the required steam can be supplied to the steam supply from the live steam network.
  • a defined pressure level in the steam supply can be ensured by the valve or throttle element.
  • the device comprises a first pressure stage, which is designed to compress condensate from the condensate return line to a third pressure level.
  • this first pressure stage is generated by a make-up pump.
  • This make-up pump can advantageously be designed in such a way that it is suitable for bringing the condensate to a pressure level of at least 12 barg, particularly preferably at least 25 barg.
  • the third pressure level will be higher than the second pressure level.
  • the third pressure level will often be between 4 bar and 15 bar higher than the second pressure level.
  • the third pressure level will be between 4.0 bar and 15.0 bar higher than the second pressure level.
  • condensate can be taken from the condensate return line, which is brought to the third pressure level by the make-up pump.
  • the heat exchanger can be connected to the first pressure stage in such a way that the condensate is further heated at the third pressure level in the heat exchanger. This heated condensate can then be at least partially evaporated, for example.
  • Table 1 pressure levels Prefers example 1 Example 2 1. Pressure level 15 - 25 barg 17 - 23 barg 18 barg 15 barg 2nd pressure level 6 - 15 barg 7 - 17 barg 9 barg 7.5 barg 3. Pressure level 5 - 25 barg 8 - 23 barg 18.2 barg 16 barg Target pressure 1.5 - 12 barg 2 - 10.0 barg 8 barg 7 barg
  • the heat exchanger can be connected to an exhaust air line in such a way that the exhaust air can be used to heat the condensate.
  • the exhaust air line is the exhaust air line of a drying device of a machine for producing or processing a fibrous web.
  • it can be the exhaust air line of the drying hood of the steam consumer according to the invention.
  • it is also possible that it is the exhaust air from a drying hood of another drying cylinder.
  • it can be provided that it is the exhaust air line of any other unit that is used in the context of the production or processing of a fibrous web.
  • the exhaust air duct of a hot air or infrared drying system of a coating installation can come into question.
  • At least one throttle element such as a fitting, a diaphragm or the like, can be provided in the device in order to at least partially evaporate the condensate after it has passed through the heat exchanger.
  • the device comprises a separator to which the at least partially evaporated condensate can be fed and to which the return line can be connected.
  • the condensate is evaporated directly at the inlet of the separator or in the interior of the separator.
  • the separator has the function of a Expansion tanks too.
  • the separator and the throttle element form a functional unit.
  • a device can be provided with which condensate can be removed from the separator and fed to the heat exchanger for evaporation.
  • This device can in particular comprise suitable lines and a second pressure-increasing device which is suitable for compressing this condensate to the third pressure level.
  • a junction can also be provided in which the condensate removed from the condensate return line can be combined with condensate which is removed from a further separator. From there, the condensate from the two sources can be fed together to the heat exchanger.
  • the two condensate flows can be compressed independently of one another and, for example, brought to the third pressure level. Then two condensate flows of the same pressure level can be mixed with one another at the junction.
  • the device according to the invention comprises only a single steam consumer, which with the Steam supply is connected.
  • the advantages of the inventive decoupling of the live steam network and the steam supply are particularly evident.
  • the steam supply is or can be connected to two or more largely identical steam consumers and / or two or more largely identical thermocompressors.
  • the second pressure level can be optimally adjusted.
  • the object is achieved by a method according to claim 10.
  • steps c) and d) are separate from one another.
  • the heated condensate does not evaporate directly in the heat exchanger, but downstream, for example by means of a throttle element.
  • the steam generated is fed into the steam supply at the second pressure level.
  • a further separator is used as a further steam source, which separator provides expansion steam at a pressure level which is below the setpoint pressure which is required for the steam consumer.
  • thermocompressor can advantageously be compressed to the desired pressure of the steam consumer and fed directly to the steam consumer.
  • thermocompressor In other applications, however, it can also be advantageous to compress the steam in the thermocompressor to the second pressure level and to feed the steam into the steam supply.
  • the at least one heat exchanger for heating the condensate exhaust air from a drying device of a machine for producing or processing a fibrous web uses a coating system.
  • the pressure level required for the steam consumer is between 6 barg and 8.5 barg. This Values are particularly advantageous when steam-heated cylinders are used as steam consumers. In special applications - e.g. with steam boxes as steam consumers - lower pressure levels (e.g. up to 1.5 barg) or possibly higher pressure levels may be necessary.
  • the values for the second pressure level and the third pressure level can be different depending on the application.
  • the second pressure level can, as already described above, be adapted to increase economic efficiency.
  • the pressure difference between the first pressure level and the second pressure level can be between 2 bar and 10 bar, in particular between 4 bar and 10 bar.
  • the pressure difference between the second pressure level and the third pressure level can advantageously be between 7.1 bar to 13 bar, in particular between 9 bar to 11 bar.
  • a separator can advantageously be provided after the evaporation of the condensate, before the generated steam is fed into the steam supply.
  • the generated steam is separated from the condensate in this separator.
  • the steam is fed from the separator into the steam supply.
  • the condensate is removed from this separator, compressed to the third pressure level by means of a second pressure stage, fed to the heat exchanger and then evaporated.
  • the condensate removed from the separator and the condensate removed from the steam consumer are brought together at a junction and fed together to the heat exchanger, with no further pressure increase occurring between the junction and the heat exchanger (5).
  • the steam consumer 1 in Figure 1 is designed as a Yankee cylinder 1, for example. According to the invention, however, other steam consumers, such as steam blow boxes, can also be provided. Steam for heating is introduced into the Yankee cylinder 1 via an inlet 1a. This steam can, for example, have a pressure level between 6 and 8.5 barg. In special applications, lower pressure levels (eg up to 3 barg) or possibly higher pressure levels may also be necessary. Condensate can be removed from the Yankee cylinder 1 via an outlet 1b. This condensate can be at a pressure level between 5 and 7.5 barg. A steam that occurs in a first separator S1 - usually a mixture of expansion steam and flow-through steam - is returned to the Yankee cylinder 1 by means of a line 12. The resulting condensate is discharged from the first separator S1 via a condensate return line.
  • thermocompressor 7 Since the pressure level of the vapor produced in the separator S1 is too low, it is compressed by means of a thermocompressor 7 to such an extent that it can be fed back into the Yankee cylinder. The thermocompressor draws the motive steam required for this from the live steam network 10
  • the embodiment shown is compressed in the thermocompressor 7 to approximately the set pressure and introduced into the steam consumer 1 via the inlet 1a.
  • the steam is compressed to the second pressure level in the thermocompressor and then introduced into the steam supply 2.
  • This second variant will usually be less favorable than the first, as more effort is required to compress the steam and more motive steam has to be used, which means that less steam can be used for heat recovery.
  • the Steam supply 2 provides steam at a second pressure level. This second pressure level is usually above the setpoint pressure with which the steam is fed into the steam consumer 1. The difference can advantageously be between 0.5 and 2.0 bar.
  • the second pressure level is 9 barg, while the setpoint pressure of the steam consumer 1 is 8 barg.
  • a heating or supplementary valve 80 can be provided upstream of the inlet 1a into the steam consumer.
  • the required second pressure level is usually well below the first pressure level made available by the live steam network 10 of the system. Therefore, in the device according to the invention, the steam supply 2 is decoupled from the live steam network 10. This decoupling takes place in the execution in Figure 1 by means of a valve 8, for example a regulating or throttle valve 8.
  • the decoupling can, however, also take place by other suitable measures, for example by a throttle element. What is essential about the decoupling is that the pressure in the steam supply 2 and the live steam network 10 can be set independently of one another. As a rule, the second pressure level of the steam supply 2 is significantly lower than the first pressure level of the live steam network 10.
  • the condensate is discharged from the first separator S1 by means of a condensate return line 3. Some of this is fed back to the steam generator 99. A part of it can, however, be used to generate steam therefrom with the aid of a heat exchanger 5. If a large amount of condensate cannot be returned to the steam generator 99, but can be evaporated again directly, the economic efficiency of the process increases considerably.
  • condensate is removed from the condensate return line 3 and brought to a third pressure level by means of a first pressure stage 4.
  • This third pressure level can, for example, be 4 to 15 bar above the second pressure level, advantageously about 7.1 to 9.5 bar above the second pressure level.
  • the absolute values of the third pressure level can be between 6 barg and 25 barg, in particular between 7 barg and 23 barg. However, the values of the third pressure level can also deviate from this in individual cases.
  • the condensate is further heated to the third pressure level.
  • the heat exchanger 5 can be operated, for example, with the exhaust air of the Yankee cylinder 1.
  • the embodiment shown by means of a throttle element 9 generates steam.
  • the steam is fed from a second separator S2 via a return line 6 into the steam supply 2.
  • the steam fed in is essentially fed in at the second pressure level. This shows an advantage of the invention once again.
  • the steam fed in does not have to be generated at the high (first) pressure level required for the motive steam, but can be generated at the (lower) second pressure level, which is usually around 1 bar above the Set pressure of the steam consumer is.
  • the condensate occurring in the second separator S2 can, as in Figure 1 shown by way of example, brought back to the third pressure level by means of a second pressure stage 11 and fed to the heat exchanger 5.
  • the condensate removed from the condensate return line 3, which is brought to the third pressure level by means of the pressure increasing device 4 - usually a pump - and the condensate removed from the separator S2 are brought together before being introduced into the heat exchanger 5.
  • the merging 15 can advantageously take place upstream of the heat exchanger 5.
  • the merging 15 preferably takes place on the pressure side of the second pump 11, that is to say after the condensate from the separator S2 has been brought to the third pressure level. In this very advantageous embodiment, there is no means for increasing the pressure of the condensate between the junction 15 and the heat exchanger 5.
  • thermocompressor 7 is taken from the steam supply 2
  • thermocompressor 7 in the embodiment in FIG Figure 1 is supplied with motive steam from the live steam network 10.
  • the second pressure level of the steam supply cannot be selected too low. Often this level can be 15 barg. With the device in Figure 1 , which is carried out according to one aspect of the invention, the second pressure level only needs to be slightly above the setpoint pressure of the steam consumer 1. Values of 9 barg and lower are not uncommon here.
  • Typical pressure levels of the two solutions are compared again in the following table: Table 2 Typical pressure levels Figure 1 Figure 2 (Hours of technology) 1. Pressure level 18 barg 18 barg 2nd pressure level 9 barg 15 barg 3. Pressure level 18.2 barg 25 barg Target pressure 8 barg 8 barg
  • the device shown differs from the device Figure 1 in that a suitable pressure-increasing device 21, for example in the form of a pump, is provided in the condensate return line 3.
  • a suitable pressure-increasing device 21 for example in the form of a pump, is provided in the condensate return line 3.
  • the condensate removed from the separator S1 is raised to a higher pressure level, namely before it is removed from the condensate return line 3 and brought to a third pressure level by means of the first pressure stage 4.
  • a pump 21 is advantageous in any case in order to convey the condensate to the steam generator.
  • higher pressures in the third pressure level can also be achieved more easily in the first pressure stage 4.
  • a level control valve 81 is also provided, which is arranged in the condensate return line 3 after the condensate has been removed.

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  • Paper (AREA)
  • Drying Of Solid Materials (AREA)

Claims (14)

  1. Machine pour la fabrication ou l'usinage d'une bande de matière fibreuse, munie d'un consommateur de vapeur (1), notamment d'un cylindre chauffé à la vapeur, dans lequel de la vapeur est introduite à une pression de consigne, d'un réseau de vapeur fraîche, qui met à disposition de la vapeur fraîche à un premier niveau de pression, et d'un dispositif pour l'alimentation du consommateur de vapeur (1), comprenant une arrivée de vapeur (2), qui met à disposition de la vapeur à un deuxième niveau de pression pour le consommateur de vapeur (1), et qui peut être reliée au réseau de vapeur fraîche (10), d'une conduite de recyclage de condensat (3) pour l'acheminement du condensat soutiré du consommateur de vapeur (1), notamment pour le recyclage dans un générateur de vapeur externe,
    d'un dispositif de génération de vapeur pour l'évaporation au moins partielle du condensat soutiré du consommateur de vapeur (1), qui comporte au moins un échangeur de chaleur (5),
    d'une conduite de réintroduction (6), qui peut être reliée à l'arrivée de vapeur (2), afin de réintroduire la vapeur générée à partir du condensat dans l'arrivée de vapeur (2), et
    d'un premier dispositif d'augmentation de la pression (4), qui est conçu pour compresser du condensat issu de la conduite de recyclage de condensat (3) à un troisième niveau de pression, l'échangeur de chaleur (5) pouvant être relié au premier dispositif d'augmentation de la pression (4) de telle sorte que le condensat au troisième niveau de pression puisse être amené dans l'échangeur de chaleur (5) pour le chauffage,
    l'arrivée de vapeur (2) pouvant être découplée du réseau de vapeur fraîche (10) et étant essentiellement constituée par un système de conduites (2) sans contenant de stockage supplémentaire, le deuxième niveau de pression de l'arrivée de vapeur (2) étant inférieur au premier niveau de pression du réseau de vapeur fraîche (10), la machine comportant en outre un thermocompresseur (7) pour l'alimentation du consommateur de vapeur (1), qui peut être relié ou est relié à un réseau de vapeur, qui met à disposition de la vapeur motrice pour le thermocompresseur (7) à un niveau de pression qui est supérieur au deuxième niveau de pression, le premier niveau de pression étant d'entre 15 et 25 barg, le deuxième niveau de pression étant d'entre 6 et 15 barg, le troisième niveau de pression étant d'entre 5 et 25 barg, et la pression de consigne étant d'entre 1,5 et 12 barg, et le deuxième niveau de pression se situant au moins 1 bar, de préférence entre 1 et 5 bar au-dessus de la pression de consigne.
  2. Machine selon la revendication 1, caractérisée en ce que le thermocompresseur (7) est relié au réseau de vapeur fraîche (10), qui met à disposition de la vapeur motrice au premier niveau de pression.
  3. Machine selon l'une quelconque des revendications précédentes, caractérisée en ce que le dispositif de génération de vapeur comporte au moins un organe d'étranglement (9), afin d'évaporer au moins partiellement le condensat après la traversée de l'échangeur de chaleur (5), ainsi qu'un séparateur (S2), dans lequel le condensat au moins partiellement évaporé peut être amené, et auquel la conduite de réintroduction (6) peut être raccordée.
  4. Machine selon l'une quelconque des revendications précédentes, caractérisée en ce que le découplage de l'arrivée de vapeur (2) du réseau de vapeur fraîche (10) a lieu au moyen d'une soupape (8), notamment d'une soupape de régulation ou d'étranglement (8) ou d'un organe d'étranglement.
  5. Machine selon la revendication 3 ou 4, caractérisée en ce qu'un dispositif est prévu, avec lequel du condensat peut être soutiré du séparateur (S2) et amené dans l'échangeur de chaleur (5), et ce dispositif comporte un deuxième dispositif d'augmentation de la pression (11), qui est approprié pour compresser le condensat au troisième niveau de pression.
  6. Machine selon l'une quelconque des revendications 3 à 5, caractérisée en ce qu'un regroupement (15) est prévu, dans lequel le condensat soutiré de la conduite de recyclage de condensat peut être regroupé avec du condensat qui est soutiré du séparateur (S2).
  7. Machine selon la revendication 6, caractérisée en ce qu'aucun moyen supplémentaire pour l'augmentation de la pression n'est prévu entre le regroupement (15) et l'échangeur de chaleur (5).
  8. Machine selon l'une quelconque des revendications précédentes, caractérisée en ce que l'échangeur de chaleur (5) peut être raccordé à une conduite d'air sortant (13) de telle sorte que l'air sortant puisse être utilisé pour le chauffage du condensat.
  9. Machine selon l'une quelconque des revendications précédentes, caractérisée en ce qu'uniquement un consommateur de vapeur unique (1) est relié à l'arrivée de vapeur (2).
  10. Procédé de récupération de vapeur d'un consommateur de vapeur (1), notamment d'un cylindre chauffé à la vapeur (1), dans une machine selon l'une quelconque des revendications précédentes, le procédé comprenant les étapes suivantes :
    a) le soutirage de condensat à partir du consommateur de vapeur (1),
    b) la compression du condensat au troisième niveau de pression,
    c) le chauffage du condensat au troisième niveau de pression dans l'au moins un échangeur de chaleur (5),
    d) l'évaporation du condensat et la génération de vapeur au deuxième niveau de pression,
    e) l'introduction de la vapeur générée dans l'arrivée de vapeur (2),
    f) la compression de vapeur de détente issue d'une source de vapeur supplémentaire au moyen du thermocompresseur au moins à la pression de consigne pour l'alimentation du consommateur de vapeur, la vapeur motrice du thermocompresseur présentant une pression qui se situe au-dessus du deuxième niveau de pression, et étant notamment soutirée du réseau de vapeur fraîche, le premier niveau de pression étant d'entre 15 et 25 barg, le deuxième niveau de pression étant d'entre 6 et 15 barg, le troisième niveau de pression étant d'entre 5 et 25 barg, et la pression de consigne étant d'entre 1,5 et 12 barg, et le deuxième niveau de pression se situant au moins 1 bar, de préférence entre 1 et 5 bar au-dessus de la pression de consigne.
  11. Procédé selon la revendication 10, caractérisé en ce que la différence de pression entre le premier niveau de pression et le deuxième niveau de pression est d'entre 2 bar et 10 bar, notamment d'entre 4 bar et 9 bar, et/ou la différence de pression entre le deuxième niveau de pression et le troisième niveau de pression est d'entre 7,1 bar et 13 bar, notamment d'entre 9 bar et 11 bar.
  12. Procédé selon la revendication 10 ou 11, caractérisé en ce que le séparateur (S2) est prévu après l'évaporation au moins partielle du condensat ou pour l'évaporation au moins partielle du condensat, avant que la vapeur générée ne soit introduite dans l'arrivée de vapeur (2).
  13. Procédé selon la revendication 12, caractérisé en ce que du condensat est soutiré du séparateur (S2), qui est compressé au troisième niveau de pression et amené dans l'échangeur de chaleur (5).
  14. Procédé selon l'une quelconque des revendications 10 à 13, caractérisé en ce qu'un séparateur supplémentaire (S1) est utilisé en tant que source de vapeur supplémentaire, qui fournit de la pression de détente à un niveau de pression qui se situe en dessous de la pression de consigne, qui est nécessaire pour le consommateur de vapeur (1).
EP18803556.2A 2017-11-10 2018-10-26 Machine de production ou de traitement d'une bande de matière fibreuse et procédé de recyclage de vapeur d'un utilisateur de vapeur dans la machine Active EP3707306B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102017126372.1A DE102017126372A1 (de) 2017-11-10 2017-11-10 Vorrichtung und Verfahren zur Trocknung einer Faserstoffbahn unter Verwendung einer Dampfrückgewinnung
PCT/EP2018/079396 WO2019091802A1 (fr) 2017-11-10 2018-10-26 Dispositif d'alimentation d'un consommateur de vapeur et procédé de récupération de vapeur d'un consommateur de vapeur

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Publication Number Publication Date
EP3707306A1 EP3707306A1 (fr) 2020-09-16
EP3707306B1 true EP3707306B1 (fr) 2021-03-31

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DE (1) DE102017126372A1 (fr)
WO (1) WO2019091802A1 (fr)

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EP2775030B1 (fr) 2013-03-06 2015-09-09 Valmet S.p.A. Dispositif de séchage d'une bande de papier mousseline et procédé de récupération de vapeur pendant le séchage d'une bande de papier tissu
EP3150761B1 (fr) 2015-09-29 2018-12-12 Voith Patent GmbH Machine pour la production ou le traitement d'une bande de matière fibreuse avec un cylindre chauffé à la vapeur et un dispositif pour alimenter le cylindre en vapeur, et méthode pour récupérer de la vapeur d'un cylindre chauffé à la vapeur d'une machine pour la production ou le traitement d'une bande de matière fibreuse

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