EP2572036A1 - Procédé et dispositif pour la récupération de chaleur dans une partie de séchage d'une machine destinée à fabriquer une bande en matière fibreuse - Google Patents

Procédé et dispositif pour la récupération de chaleur dans une partie de séchage d'une machine destinée à fabriquer une bande en matière fibreuse

Info

Publication number
EP2572036A1
EP2572036A1 EP11704067A EP11704067A EP2572036A1 EP 2572036 A1 EP2572036 A1 EP 2572036A1 EP 11704067 A EP11704067 A EP 11704067A EP 11704067 A EP11704067 A EP 11704067A EP 2572036 A1 EP2572036 A1 EP 2572036A1
Authority
EP
European Patent Office
Prior art keywords
steam
condensate
pressure
line
drying cylinder
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP11704067A
Other languages
German (de)
English (en)
Inventor
Raffaele Mancini
John C. Denison
Marco Popp
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Voith Patent GmbH
Original Assignee
Voith Patent GmbH
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Voith Patent GmbH filed Critical Voith Patent GmbH
Publication of EP2572036A1 publication Critical patent/EP2572036A1/fr
Withdrawn legal-status Critical Current

Links

Classifications

    • 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
    • D21F5/02—Drying on cylinders
    • 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
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
    • Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working

Definitions

  • the invention relates to a method for heat recovery for a dryer section of a machine for producing a fibrous web, in particular a paper, board or tissue web, wherein the fibrous web is dried at least with a steam-heated drying cylinder and at least one high-temperature hood with hot air, wherein the at least one drying cylinder at least partially supplied with live steam, wherein the condensate / steam mixture of the at least one drying cylinder is fed to a condensate separator, wherein the steam from the Kondensatabscheider the live steam or a live steam / high pressure steam mixture is supplied, wherein at least a portion of the condensate from the at least one Drying cylinder downstream condensate is fed to a heat exchanger in the exhaust air stream of the high-temperature hood, and wherein the condensate is heated there and absorbs energy of the exhaust air, followed by a pressure-reducing element en is tensions and thereby at least partially evaporated again.
  • the invention relates to a device for heat recovery for a dryer section of a machine for producing a fibrous web, in particular a paper, board or tissue web, in which a fibrous web is dried, consisting of at least one steam-heated drying cylinder and at least one high-temperature hood which acts with hot air wherein the at least one drying cylinder is at least partially supplied with live steam, wherein the condensate / vapor mixture of the at least one drying cylinder is fed to a condensate separator, wherein the steam from the condensate is fed to the live steam or a live steam / high pressure steam mixture, wherein at least a portion of the condensate from the at least one drying cylinder downstream condensate is fed to a heat exchanger in the exhaust air stream of the high temperature hood, and wherein the condensate is heated there and energy of the Exhaust air absorbs, is subsequently relaxed by a pressure-reducing element and thereby at least partially evaporated again.
  • Such a method or such a device is known for example from the document AT 506 077 B1.
  • a method and apparatus for heat recovery in a dryer section of a paper machine wherein a paper web is dried with a steam heated drying cylinder and a hot air supplied high temperature hood and exhaust steam from a steam system is fed to a vapor separator, wherein a portion of the condensate from the vapor separator in a a separate circuit is recycled via a heat exchanger back into the same and single steam separator and the condensate is supplied via the heat exchanger heat from the exhaust air of the high-temperature hood.
  • the invention had the object of providing an improved and easier controllable heat recovery process available.
  • the improvement seen by the applicant there compared to the prior art is that the heating of the condensate in the heat exchanger mentioned does not have to result completely in evaporation, since the steam, or else the vapor / condensate mixture, is returned to the said condensate separator.
  • the document DE 35 01 584 A1 discloses a device on a dryer section of paper machines, which consists of drying cylinders and at least one high-temperature hood.
  • the invention in this Registration was based on the object to use the energy content of the exhaust air and thereby reduce the primary energy use for drying.
  • the inventive solution should be retrofittable to existing systems.
  • this object is achieved in that the cylinder is connected in a conventional manner, a vapor separator for separating the exhaust steam, wherein on the one hand the steam separator is connected to a Schlupfdampf admir and a compressor to the feed line to the drying cylinder, and on the other hand, the condensate line of the vapor separator is connected via the heat exchanger of the high temperature hood with the Schlupfdampf admir.
  • the present invention has for its object to improve a method and an apparatus of the aforementioned types for heat recovery in such a way over the prior art that the offered energy of the exhaust air flow of at least one high-temperature hood is used thermodynamically at the highest possible level.
  • thermodynamic advantage is that the condensate can be heated to a very high temperature in the heat exchanger, resulting in a very high vapor pressure after recuperation. Because the resulting vapor is fed into a steam line or vapor vessel, the pressure of which is higher than the pressure of the condensate downstream of the at least one drying cylinder, there is no system-limited limit on the pressure of the resulting vapor, as is the case, for example would feed the steam in a condensate, which is immediately downstream of a drying cylinder and therefore there must prevail the condensate side pressure of the drying cylinder.
  • Another advantage is that the entire heat recovery system without compressor, which are located in a steam-containing line, gets along.
  • the steam line or the steam tank into which the high-pressure steam is fed be the line is guided in the live steam.
  • the steam line or the steam tank, in which the high-pressure steam is fed be the line in which the steam mixture of live steam and steam from the at least one drying cylinder downstream condensate is performed.
  • the resulting condensate, which can form in the second condensate, is advantageously, at least partially, again supplied to the heat exchanger.
  • the condensate that comes from the second condensate can be reheated and thus can form a higher temperature of the condensate, which in turn can lead to a higher pressure on the second Kondensatabscheider, or to a higher pressure possible high pressure steam.
  • the resulting condensate which may form in the second condensate separator, may alternatively be supplied via a pressure-reducing element to at least a portion, preferably for the most part, the condensate separator to which the condensate / vapor mixture of the at least one drying cylinder is also fed, so that the condensate of the second condensate can evaporate via this pressure-reducing element.
  • the resulting condensate which may form in the second condensate separator, may alternatively be supplied at least in part, preferably for the most part, to a third condensate separator via a pressure-reducing element, which may be a diaphragm or, preferably, a valve.
  • a pressure-reducing element which may be a diaphragm or, preferably, a valve.
  • this steam can be fed into the line in which the steam mixture of live steam and steam is passed out of the at least one drying cylinder downstream condensate.
  • This variant has the thermodynamic advantage that the heated by the heat exchanger condensate can evaporate in two stages, each of which is higher than the pressure of the at least one drying cylinder downstream condensate.
  • the heated condensate from the heat exchanger can be fed via the second Kondensatabscheider as high pressure steam in the live steam, and the still hot condensate from the third Kondensatabscheider can be fed as steam in the line in which the steam mixture of live steam and steam out of the at least one drying cylinder downstream condensate.
  • the vapor of the third condensate can be combined with the steam of the at least one drying cylinder downstream condensate.
  • the third condensate separator and the condensate separator downstream of the at least one drying cylinder would be interconnected in a communicating manner. Communicating means in this context without closed shut-off devices; It is possible that prevail in both condensate equal pressure conditions.
  • This variant is particularly suitable for conversions of the heat recovery system, since the capacity of an existing condensate, which is connected downstream of the at least one drying cylinder, can continue to be used.
  • the third condensate separator fulfills the function described above and, in effect, extends the capacity of the existing condensate separator.
  • a valve is used as a pressure-reducing element after the heat exchanger for the expansion of the condensate, then there is the advantage that the pressure downstream of the pressure-reducing element, and thus the pressure at the second condensate separator, can be influenced.
  • a valve is used as a pressure-reducing element after the heat exchanger for the expansion of the condensate, this can be advantageously controlled according to a pressure setpoint, the pressure actual value of which represents the pressure at the second condensate separator.
  • the pressure can be ideally measured at the second condensate separator, since this belongs to the so-called controlled system of the valve.
  • This pressure setpoint can now be generated automatically in a further embodiment according to the Druckist- / or pressure setpoint in the steam line or the steam tank, the pressure of which is higher than the pressure of the at least one drying cylinder downstream condensate.
  • a value can be generated which is greater than the pressure setpoint or pressure setpoint in the steam line or the steam container, the pressure of which is higher than the pressure of the condensate separator downstream of the at least one drying cylinder. It is thus achieved that in außpendelten operating state of the generated high-pressure steam can flow safely.
  • a valve is used as a pressure-reducing element after the heat exchanger for the expansion of the condensate, so can be controlled alternatively to the aforementioned control versions to a pressure setpoint whose actual pressure is the condensate pressure on or after the heat exchanger. After the heat exchanger is called here between the heat exchanger and said pressure-reducing valve.
  • This alternative control would have the advantage that the pressure of the condensate in the heat exchanger can be kept so high explicitly via the pressure-reducing valve that unwanted evaporation of the condensate at the heat exchanger is prevented. It is also advantageous that unwanted return flow of steam of the steam line or the steam tank, the pressure of which is higher than the pressure of the at least one drying cylinder downstream condensate to prevent mechanically into the high-pressure steam.
  • a non-return valve preferably a check valve, could prevent the undesirable backflow.
  • the condensate does not evaporate in the heat exchanger. Vaporizing already in the heat exchanger would be an unwanted operating condition and, moreover, would considerably impair the heat transfer in the heat exchanger.
  • the pressure of the condensate is raised to a sufficient pressure level, so that it is ensured that the condensate does not evaporate unintentionally.
  • a pump upstream of the heat exchanger can be used.
  • the generation of hot condensate via the heat exchanger is largely determined by the energy offered in the exhaust air stream of the high-temperature hood.
  • Operating conditions, in particular safety-relevant requirements, can lead to bypassing, or at least partially bypassing, the exhaust air of the high-temperature hood around the heat exchanger.
  • an exhaust bypass system can prevent unwanted overheating of the condensate by passing the exhaust air from the high-temperature hood through a bypass on the heat exchanger.
  • the object of the invention is achieved in a device of the type mentioned above in that the heated by the heat exchanger condensate, which is subsequently relaxed by a pressure-reducing element and thereby at least partially evaporated again over at least one line is connected as high pressure steam to a steam line or a steam tank, the pressure of which is higher than the pressure of the at least one drying cylinder downstream condensate.
  • the thermodynamic advantages of the device arise in accordance with the thermodynamic advantages of the method according to the invention.
  • the device according to the invention dispenses with compressors which are located in lines containing steam. This is advantageous from an investment as well as from an operating cost point of view.
  • the pressure-reducing element is advantageously followed by a second Kondensatabscheider.
  • This condensate separator allows non-evaporated condensate to collect there specifically.
  • the steam line or the steam tank into which the high-pressure steam is fed be the line is guided in the live steam.
  • the steam line or the steam tank, in which the high-pressure steam is fed be the line in which the steam mixture of live steam and steam from the at least one drying cylinder downstream condensate is performed.
  • the conduit which carries the condensate from the second condensate separator is connected to the conduit to the heat exchanger.
  • This thermodynamically has the advantage that the already heated condensate from the second condensate can be driven again over the heat exchanger. In continuous operation of the system can thus set a desired pressure level in the second condensate.
  • the conduit which carries the condensate from the second condensate separator may be connected to the condensate separator, which is also supplied with the condensate / vapor mixture of the at least one drying cylinder, wherein a pressure-reducing element, preferably a valve or orifice, is located in this conduit ,
  • a pressure-reducing element preferably a valve or orifice
  • conduit which carries the condensate from the second condensate separator may be connected to a third condensate separator.
  • a pressure-reducing element preferably a valve or a diaphragm may be located.
  • the line that carries steam from this third condensate separator can be connected to various other lines.
  • the line leading from this third condensate vapor can be connected to the line in which the vapor mixture of live steam and steam from the at least one drying cylinder downstream condensate is performed.
  • This variant has the thermodynamic advantage that the heated by the heat exchanger condensate can evaporate in two stages, each of which is higher than the pressure of the at least one drying cylinder downstream condensate.
  • the heated condensate from the heat exchanger can be fed via the second Kondensatabscheider as high pressure steam in the live steam, and the still hot condensate from the third Kondensatabscheider can be fed as steam in the line in which the steam mixture of live steam and steam out of the at least one drying cylinder downstream condensate.
  • This variant is particularly suitable for conversions of the heat recovery system, since the capacity of an existing condensate, which is connected downstream of the at least one drying cylinder, can continue to be used.
  • the pressure-reducing element is advantageously designed as a valve.
  • a valve has the advantage that the pressure gradient can be adjusted specifically at this point.
  • An orifice whose geometric flow area is designed according to the operating conditions and the desired pressure gradient can be used as a pressure-reducing element as an alternative to a valve.
  • a mechanical check element preferably a mechanical check valve
  • the high-pressure steam has a greater pressure than, for example, the live steam should high-pressure steam flow into the line of live steam. If the high-pressure steam is lower in pressure than the live steam, it is intended to prevent fresh steam from flowing into the high-pressure steam through the mechanical non-return element. However, it is also a controlled valve that takes over the function of the check valve, conceivable in this position.
  • the heat exchanger is advantageously preceded by a pump which is able to produce a pressure of condensate to the heat exchanger, which is higher than the temperature corresponding evaporation pressure of the condensate in the heat exchanger.
  • the pressure of the condensate can be explicitly set via the pump in such a way that no unwanted vaporization occurs at a given temperature of the condensate.
  • Figure 1 is a schematic representation of a preferred embodiment
  • Figure 2 is a further schematic representation of a preferred embodiment
  • Figure 3 is a further schematic representation of a preferred embodiment
  • Figure 4 is a further schematic representation of a preferred embodiment
  • Figure 5 is a further schematic representation of a preferred embodiment
  • FIG. 6 A further schematic representation of a preferred embodiment
  • Figure 7 is a further schematic representation of a preferred embodiment
  • Figure 8 is a further schematic representation of a preferred embodiment
  • FIG. 1 shows a preferred embodiment according to the invention in which a fibrous web F is dried.
  • the fibrous web F is guided around a drying cylinder 1, which is supplied with steam. It is too to detect a high-temperature hood L1, which acts on the fibrous web F with hot air.
  • the air system of the high-temperature hood L1 has a circulation fan L3 with a subsequent gas burner L2 for heating the circulating air L4 performed. It is a large part of the circulating air L4, which is guided by the high-temperature hood L1, circulated directly in this recirculation system. Since the circulating air L4 can absorb only a finite degree of water, circulating circulating air L4 is partially removed via the exhaust air system and replaced by supply air L7.
  • the exhaust air system consists of an exhaust fan L5 and several heat exchangers W1 and L8. Heat exchangers L8 may be a plurality of heat exchangers for warming up process water or for heating air, such as supply air L7 for high temperature hood L1.
  • the heat exchangers L8 are not obvious from this invention, the use is not discussed in more detail.
  • a heat exchanger W1 whose function is related to the invention.
  • condensate is heated from a steam and condensate system.
  • the exhaust air L6 can be passed to the heat exchanger W1 wholly or partially by an exhaust air bypass system.
  • the exhaust air bypass system can be switched so that the whole exhaust air L6 is passed through the heat exchanger W1.
  • the steam and condensate system feeds the drying cylinder 1 with steam, which may be a mixture of different steam pressure stages and steam from different heat recovery stages.
  • the steam D1, 2,3, which is supplied to the drying cylinder 1, condenses due to the heat transfer through the drying cylinder 1 to the fibrous web F and is discharged as condensate / vapor mixture K1 from the drying cylinder 1.
  • the condensate / vapor mixture K1 from the drying cylinder 1 is fed to a first condensate separator A1.
  • this first condensate A1 contained steam from the condensate / vapor mixture K1 from the Drying cylinder 1 ascend as separated steam.
  • condensate can re-evaporate due to the pressure conditions in the first condensate A1 and rises as so-called Brüdendampf.
  • the separated steam and the so-called Brüdendampf then yield the steam D3 from the first condensate A1.
  • the steam D3 from the first condensate separator A1 is fed via a so-called thermocompressor TK1 as low-pressure steam according to the injector principle into the main steam / high-pressure steam mixture D1, 2.
  • the vapor D3 from the first condensate separator A1 has a lower pressure than the live steam / high pressure steam mixture D1, 2.
  • the condensate K2 from the first condensate separator A1 can be pumped via a pump P1 to a steam generator.
  • the steam generator may be, for example, a boiler house or other steam generator, which is not shown in this figure.
  • Another part of the condensate K3 from the first condensate separator A1 is conveyed via another pump P2 for later steam generation directly or indirectly to the heat exchanger W1.
  • condensate K4 of a second condensate trap A2 is fed to this condensate K3.
  • the pump P3 conveys the condensate K3,4 and increases the pressure such that the condensate K3,4 does not evaporate in the heat exchanger W1 despite heating in the heat exchanger W1.
  • the pressure of the heated condensate K * 3.4 from the heat exchanger W1 is only, and explicitly, degraded via a pressure-reducing element DR1.
  • the pressure of the condensate K * 3.4 from the heat exchanger W1 is reduced above the pressure-reducing element DR1 such that the condensate K * 3.4 evaporated.
  • the pressure-reducing element DR1 can be designed as a regulated valve or as a diaphragm.
  • the resulting at the pressure reducing element DR1 steam is supplied to said second condensate A2. It may be reflected in the second condensate A2 of this resulting steam in part again as condensate, as must build for thetientpendelten operating condition of the system, a pressure in the second condensate A2, which is large enough to overcome the back pressure of live steam D1 at the check valve R1.
  • the exemplary check valve R1 is installed so that no steam from the live steam line D1 can get into the line of high-pressure steam D2; the direction of flow is from high pressure steam D2 to live steam D1.
  • the check valve R1 could also be designed as a controllable valve, which is a control deposited, which releases the valve only when electronically queried operating conditions and optionally drives the valve to certain degrees of opening.
  • the now optionally formed live steam / high pressure steam mixture D1, 2 is now passed through a thermocompressor TK1.
  • FIG. 2 shows a further schematic representation of a preferred embodiment of the invention, which differs in the following features from FIG. 1:
  • the condensate K3 from the first condensate separator A1 is required by a pump P2 to the heat exchanger W1. It eliminates in this embodiment, the pump P3 for pressure increase.
  • the condensate K4 from the second condensate A2 passes via a line to a pressure-reducing element DR2 before the first condensate A1, so that the condensate K4 can evaporate due to the pressure-reducing element DR2 and enters the condensate A1.
  • FIG. 3 shows a further schematic representation of a preferred embodiment of the invention, which differs in the following features from FIG. 1:
  • the feed point, in which the high-pressure steam D2 is fed, is located in the line in which the steam mixture of live steam D1 and steam D3 is led out of the first condensate separator A1.
  • FIG. 4 shows a further schematic illustration of a preferred embodiment of the invention, which differs in the following features from FIG. 2:
  • FIG. 5 shows a further schematic representation of a preferred embodiment of the invention, which differs in the following features from FIG. 1:
  • the high-pressure steam D2 is conducted to applications other than the steam and condensate system shown here.
  • FIG. 6 shows a further schematic illustration of a preferred embodiment of the invention, which differs in the following features from FIG. 2:
  • FIG. 7 shows a further schematic representation of a preferred embodiment of the invention, which differs in the following features from FIG. 1:
  • the condensate K4 from the second condensate A2 is not merged with the condensate K3 from the first condensate A1, but passed into a third condensate A3.
  • a pressure-reducing element DR3 preferably a controlled valve or an orifice, which allows the condensate K4 from the second condensate A2 relaxed in the third condensate A3 and thereby can evaporate again.
  • the resulting vapor D4 from the third condensate A3 is passed through a check element R2 in the line in which the vapor mixture of live steam D1 and steam D3 is guided out of the first condensate A1.
  • the condensate K5 from the third condensate A3 is guided into the line in which the condensate K3 is from the condensate A1. Accordingly, the condensate K5 and condensate K3 are led together to the heat exchanger.
  • FIG. 8 shows a further schematic illustration of a preferred embodiment of the invention, which differs in the following features of FIG. 2:
  • the condensate K4 from the second condensate separator A2 is not combined with the condensate K3 from the first condensate separator A1, but into a third condensate separator A3 headed.
  • a pressure-reducing element DR3 preferably a controlled valve or an orifice, which allows the condensate K4 from the second condensate A2 relaxed in the third condensate A3 and thereby can evaporate again.
  • the resulting vapor D4 from the third condensate A3 is fed into the line in which the steam D3 is guided out of the condensate A1.
  • the resulting vapor D4 from the third condensate A3 can also be led to other steam consumers, which are not shown in this figure.

Abstract

L'invention concerne un procédé pour la récupération de chaleur dans la partie de séchage d'une machine destinée à fabriquer une bande en matière fibreuse (F), en particulier une bande en papier, carton ou tissu ouaté, la bande en matière fibreuse (F) étant séchée à l'air chaud au moins à l'aide d'un cylindre de séchage (1) chauffé à la vapeur et d'au moins un capot à haute température (L1). Ledit au moins un cylindre de séchage (1) est alimenté au moins partiellement en vapeur fraîche (D1). Le mélange condensat/vapeur (K1) dudit au moins un cylindre de séchage (1) est introduit dans un séparateur de condensat (A1). La vapeur (D3) sortant du séparateur de condensat (A1) est introduite dans la vapeur fraîche (D1) ou dans un mélange vapeur fraîche/vapeur haute pression (D1,2). Au moins une partie du condensat (K3) du séparateur de condensat (A1) disposé en aval dudit au moins un cylindre de séchage (1) est introduite dans un échangeur de chaleur (W1) disposé dans le flux d'air résiduaire (L6) du capot à haute température (L1). Le condensat (K3,4) y est chauffé et y absorbe l'énergie de l'air résiduaire (L6), il est ensuite détendu par un élément réducteur de la pression (DR1) et s'évapore de ce fait à nouveau partiellement. Le procédé selon l'invention est caractérisé en ce que le condensat (K*3,4) chauffé par l'échangeur de chaleur (W1), qui a ensuite été détendu par un élément réducteur de pression (DR1) et de ce fait à nouveau au moins partiellement évaporé, est injecté au moins partiellement en tant que vapeur haute pression (D2) dans une conduite de vapeur ou un récipient à vapeur, dont la pression est supérieure à la pression du séparateur de condensat (A1) disposé en aval dudit au moins un cylindre de séchage (1). La demande concerne également un dispositif (100) pour la réalisation du procédé selon l'invention.
EP11704067A 2010-05-19 2011-02-17 Procédé et dispositif pour la récupération de chaleur dans une partie de séchage d'une machine destinée à fabriquer une bande en matière fibreuse Withdrawn EP2572036A1 (fr)

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
DE102010029132 2010-05-19
DE102010031271 2010-07-13
DE102010041231A DE102010041231A1 (de) 2010-05-19 2010-09-23 Verfahren und Vorrichtung zum Verfahren zur Wärmerückgewinnung für eine Trockenpartie einer Maschine zur Herstellung einer Faserstoffbahn
PCT/EP2011/052332 WO2011144366A1 (fr) 2010-05-19 2011-02-17 Procédé et dispositif pour la récupération de chaleur dans une partie de séchage d'une machine destinée à fabriquer une bande en matière fibreuse

Publications (1)

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EP2572036A1 true EP2572036A1 (fr) 2013-03-27

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EP11704067A Withdrawn EP2572036A1 (fr) 2010-05-19 2011-02-17 Procédé et dispositif pour la récupération de chaleur dans une partie de séchage d'une machine destinée à fabriquer une bande en matière fibreuse

Country Status (4)

Country Link
EP (1) EP2572036A1 (fr)
CN (1) CN103025955A (fr)
DE (1) DE102010041231A1 (fr)
WO (1) WO2011144366A1 (fr)

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Publication number Priority date Publication date Assignee Title
CN105926341A (zh) * 2016-04-27 2016-09-07 陕西科技大学 一种卫生纸机干燥部能耗协同装置及其控制系统
CN105926341B (zh) * 2016-04-27 2017-08-29 陕西科技大学 一种卫生纸机干燥部能耗协同装置及其控制系统

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