WO2010091765A1 - Vorrichtung und verfahren zum trocknen einer tissuepapierbahn mit dampfrückgewinnung - Google Patents
Vorrichtung und verfahren zum trocknen einer tissuepapierbahn mit dampfrückgewinnung Download PDFInfo
- Publication number
- WO2010091765A1 WO2010091765A1 PCT/EP2009/067753 EP2009067753W WO2010091765A1 WO 2010091765 A1 WO2010091765 A1 WO 2010091765A1 EP 2009067753 W EP2009067753 W EP 2009067753W WO 2010091765 A1 WO2010091765 A1 WO 2010091765A1
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- WIPO (PCT)
- Prior art keywords
- condensate
- pressure level
- bar
- hot air
- cylinder
- Prior art date
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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
Definitions
- the present invention relates to
- Tissue Textilherstellimg and in particular a device for drying a tissue paper web with a heated cylinder, the so-called.
- Yankee or crepe cylinder which is fed to heat it from a live steam network steam, and a hot air hood on the outer circumference of the cylinder to blow hot air onto the tissue paper web and suction, wherein the tissue paper web is dried by both the hot outer surface of the cylinder and the hot air.
- the evaporated water is sucked off and disposed of via the exhaust air of the hot air hood.
- the present invention relates to a method for vapor recovery when drying a tissue paper web with such a device.
- tissue paper a soft absorbent paper with a low basis weight.
- a weight per unit area of 8 to 40 g / m s , in particular 10 to 25 g / m 2 is selected.
- the total basis weight of a multi-ply tissue product is preferably up to a maximum of 120 g / m 2 , more preferably up to a maximum of 60 g / m 2 .
- Its density is typically below 0.6 g / cm 3 , preferably below 0.30 g / cm 3, and more preferably between 0.08 and 0.20 g / cm 3 .
- tissue paper differs from papermaking by the extremely low basis weight and the much higher tensile breaking index (see DIN EN 12625-4 and DIN EN 12625-5). Paper and tissue also generally differ in terms of modulus of elasticity, which is the same Stress-strain properties of these planar products are characterized as material parameters.
- the high pull tear work feature comes from the outer or inner creping of the tissue.
- the former creping is performed by compression of the paper web on a dry cylinder as a result of the action of a creping doctor or, in the case of the latter creping, as a result of a difference in speed between two fabrics, causing the still-moist, plastically deformable Paper web is broken up internally by compression and shearing, making it more stretchable under load than an uncreped paper.
- Wet tissue paper webs are usually dried by so-called Yankee drying, through air drying (TAD) or pulse drying.
- TAD through air drying
- pulse drying pulse drying
- the fibers contained in the tissue paper are mainly cellulosic fibers, such as chemical fiber pulp fibers (eg, kraft pulp and
- tissue paper may also include other types of fibers, e.g., regenerated cellulosic fibers or synthetic fibers. which increase, inter alia, the strength, absorbency, smoothness or softness of the tissue paper.
- Dxe use of a steam-heated cylinder and a hot air hood is blown by means of the hot air to the running around the heated cylinder tissue web, in the prior art z.
- the object of the present invention is therefore to provide a device for drying a tissue paper web as well as a method for Dampfruckgewmnung when drying a tissue paper web, which make it possible to reduce the amount of steam required to dry the tissue paper web from a live steam network m a stable control loop, in particular at To reduce the paper production and in particular the drying costs incurred.
- the invention is based on the idea of using the exhaust air from the hot air hood, which has already been used for drying the tissue paper web, but has a high residual energy content, to evaporate condensate from the heated cylinder and the steam generated at a higher pressure level to feed back the fresh steam network.
- a live steam network is a big buffer, making a more stable Loop can be achieved with the associated stable drying and thus stable paper quality.
- the device for drying a tissue paper web comprises a heatable cylinder, the so-called Yankee or crepe cylinder.
- the cylinder is connected for heating with steam to a supply line which supplies the steam and which can be connected to a live steam network.
- a live steam network means any mains that provides live steam and supplies at least two consumers with live steam at a first pressure level.
- One of the consumers is the heatable cylinder of a tissue paper machine.
- the other consumer can z. B. also be a heatable cylinder but another tissue paper machine. But other consumers are also conceivable.
- the condensate formed in the cylinder during drying is removed from the cylinder via a condensate line.
- the device comprises a hot air hood on the outer circumference of the cylinder to blow hot air in the direction of the outer periphery and thus in operation on the running around the heated cylinder tissue paper web.
- the tissue paper web is dried on the one hand by the hot outer circumference of the heated cylinder and on the other hand by the blown on the tissue paper web hot air of the hot air hood.
- the hot air of the hot air hood After the hot air of the hot air hood has been used to dry the tissue paper, it is removed with the evaporated water via an exhaust air line from the hot air hood.
- the device according to the invention further comprises a first pressure stage, which is designed to compress condensate from the cylinder to the first pressure level of the Yankee cylinder.
- an evaporation device for at least partial evaporation of the condensate is provided with an energy transfer device.
- the energy transfer device is configured to generate energy Exhaust air in the exhaust duct to transfer to the condensate.
- the energy transfer can be adversely affected by the presence of vapor bubbles in the condensate ,, so that the energy transfer according to the invention takes place downstream of the first pressure stages. Increasing the pressure increases the boiling point of the condensate (water) and thus prevents the occurrence of vapor bubbles in the heat exchanger.
- the device of the present invention comprises a recirculation line, which is connectable to the main steam network to feed back steam generated from the condensate into the main steam network. Due to the inventive design, the exhaust air from the hot air hood or its energy is used to generate steam from the condensate discharged from the cylinder, so that less live steam from a live steam network is needed, whereby the energy or live steam costs can be reduced. Furthermore, the live steam network provides a sufficiently large buffer to provide a stable control loop necessary to achieve a constant temperature of the heated cylinder with the associated consistent dry quality and paper quality.
- a second pressure stage which is designed to remove the condensate from the substantially first pressure level to compress to a second higher pressure level.
- the boiling temperature is further increased, thereby condensing possible vapor bubbles in the condensate and the occurrence of vapor bubbles is essentially excluded.
- the energy transfer device is consequently connected downstream of the second pressure stage and preferably formed by a heat exchanger arranged in the exhaust air, in particular a tube heat exchanger.
- the condensate, which has been compressed to the second pressure level is heated via the heat exchanger.
- a third pressure stage which is designed to suddenly and suddenly vaporize the heated condensate, for which purpose the condensate is expanded from the second pressure level to the first pressure level, ie the evaporation takes place primarily in that the pressure level of the previously heated condensate is reduced so that the boiling temperature abruptly decreases and is thus exceeded and a phase transition from liquid to gas takes place.
- the expansion is intended to bring the generated steam to the pressure level of the live steam network to allow a return feed via the return line.
- the device further comprises a first Kondensatabscheider which communicates with the condensate line and a first condensate connected to the first return line.
- the first pressure stage is formed by a first pump in the first return line.
- a second condensate separator is provided, which is in communication with the first return line.
- the condensate is preferably introduced via a diffuser in the second condensate. Furthermore, a second return line is provided which is connected to the second condensate separator.
- the second pressure stage is in this case formed by a second pump in the second return line and the heat exchanger is the second pump downstream integrated into the second return line.
- the third pressure stage is according to this embodiment, preferably by a Heat exchanger arranged downstream
- Expansion device formed in the form of an expansion valve or a capillary or throttle in the second return line. Furthermore, the second return line of the expansion device is connected downstream of the second condensate separator. The return of the generated steam is also from the second condensate, to which the return feed line is connected to this.
- the second pressure level is preferably in the range of 23-27 bar, preferably in the range of 24-26 bar, and most preferably 25 bar. This pressure range is selected so that, when passing through the heat exchanger m depending on the heat transferred to the condensate, the boiling temperature is not exceeded and thus no steam is generated. This is to be generated according to the preferred form of export from the expansion only in the third pressure stage.
- the first pressure level is in the range of 10-15 bar, preferably 13-14 bar, and most preferably 13 bar, depending on the pressure of the live steam network.
- Energy transfer device comprises a Kondensatabscheider through which the exhaust pipe preferably extends with a large surface, so that the heat transfer is transferred from the exhaust air to the condensate in the condensate, whereby the condensate evaporates in the condensate.
- the steam generated in the condensate is also returned via the return supply line into the main steam network.
- the condensate separator with its large dimensions and its high weight must be placed in a high position, ie above the paper machine. This can lead to constructive and constructional problems.
- Advantage of this embodiment can be dispensed with pumps and valves.
- high-temperature hoods as hot air hoods, as described for example in EP 0 905 311 A2.
- Such hot air hoods are designed to blow hot air having a temperature of more than 53O 0 C on the tissue paper web. At the moment, a maximum of 65O 0 C is achieved.
- the exhaust air of such a high-temperature hood has a temperature of about 150 ° C. less than the hot air and is therefore at most 500 ° C.
- a method for producing steam during drying of a tissue paper web with a cylinder fed from a live steam network and a hot air hood which flows hot air onto the tissue paper web.
- the inventive method comprises the steps of removing condensate from the cylinder, compressing the condensate to a first pressure level corresponding to that of the fresh steam network, heating the condensate by noise exchange with the exhaust air from the hot air hood, evaporation of the condensate and feeding the steam generated in the live steam network.
- the condensate it is preferred to compress the condensate after compression to the pressure level and before heating the condensate with exhaust air from the hot air hood to a second higher pressure level, whereby the boiling temperature of the condensate (water) is raised and thus the occurrence of Steam bubbles is reduced.
- a second higher pressure level whereby the boiling temperature of the condensate (water) is raised and thus the occurrence of Steam bubbles is reduced.
- the condensate does not evaporate during the heat transfer from the exhaust air to the condensate, ie the pressure level is chosen sufficiently high and the evaporation takes place only after the heating of the condensate with exhaust air from the hot air hood by relaxation to the first pressure level.
- the pressure ranges of the second and first pressure levels correspond to the above-mentioned pressure ranges as well as the exhaust air preferably has a temperature of more than 350 0 C.
- Fig. 1 shows a schematic diagram of an inventive device in a first embodiment
- Fig. 2 shows a schematic diagram of an inventive device in a second embodiment.
- a live steam power line 12 is shown, which is to represent the live steam network, from which the Yankee cylinder 10 is supplied with steam.
- the live steam network 12 provides live steam at a pressure of approximately 13 bar.
- the live steam network 12 and the Yankee cylinder 10 are connected to each other via a supply line 13.
- a pressure reduction via an expansion device 14 takes place.
- the steam supplied to the Yankee cylinder 10 at a pressure of 6-8 bar heats the Yankee cylinder 10 so that the tissue paper web (not shown) guided around the outer surface or part of the outer surface of the Yankee cylinder 10 is dried by heat conduction ,
- the exhaust air is through an exhaust passage 15 via a bypass 40 with a flap 42 to open the bypass or close, on the blower 16 for hot water production, for heating the machine hall, in which the paper machine is, for Frischluftvorwarmung or to further Warmeruck alongungsiker the blower 16 derived.
- the exhaust air via the exhaust duct 15 with the flap 43 open via the line 41 through a built-in exhaust pipe 15 heat exchanger 38 to flow before it is supplied via the blower 16 to the aforementioned heat recovery measures.
- the heat exchanger 38 may be a conventional pipe heat exchanger.
- Saturated steam temperature is in a pressure range discharged between about 5-6 bar from the Yankee cylinder 10.
- a condensate line 17 is provided.
- the condensate line 17 opens into a first condensate separator 18, in which condensate is separated from steam.
- the upper portion of the Kondensatabscheiders 18 is further connected via a line 19 with a thermocompressor 20 (jet pump), which can be brought via a line 21 and a valve 23 with the live steam line 12 in fluid communication.
- the condensate 22 vapor water
- the condensate 22 collects, ie water, which is located substantially in the vicinity of the saturated steam temperature.
- the condensate is passed through an expansion device (26). a collecting container (not shown) supplied.
- the lower region of the first condensate separator 18 for discharging the condensate 22 is connected to a first return line 25.
- the condensate 22 in the first condensate separator 18 can flow into the first return line 25. Downstream of the valve 27, a first pump 28 is arranged (first pressure stage). The pump 28 leads to a compression of the condensate 22 to a pressure of about 13.5 bar and conveys the condensate to a second Kondensatabscheider 29. At the inlet of the second Kondensatabscheiders 29, the condensate has about a pressure of 13 bar and a temperature between about ISO 0 C and 16O 0 C. However, prevails in the second Kondensatabscheider 29 (as described later) a temperature of about 180 to 190 0 C.
- the condensate from the return line 25th introduced via a diffuser 30 in the second Kondensatabscheider 29 Due to the temperature difference between the introduced condensate and the medium in the second Kondensatabscheider 29, the condensate from the return line 25th introduced via a diffuser 30 in the second Kondensatabscheider 29.
- the lower section of the second condensate 29 collects substantially liquid condensate 31.
- the lower portion of the second Kondensatabscheiders 29 is connected to a second return line 33.
- a second pump 34 second pressure stage
- the second pump 34 compresses the condensate 31 from the second Kondensatabscheider 29 to a pressure of about 25 bar.
- the compressed condensate downstream of the pump 34 is located approximately in a temperature range of about 18O 0 C to 19O 0 C, flows through the heat exchanger 38.
- energy is transferred from the exhaust air in the exhaust duct 15 to the condensate in the return line 33 and the condensate is heated.
- the pressure of the condensate is selected to be so high that during the heating of the condensate no evaporation of the condensate and in particular no vapor bubbles arise.
- the condensate Downstream of the heat exchanger 38, the condensate has a temperature of about 209 0 C at a pressure of 25 bar.
- an expansion valve 35 is provided downstream of the heat exchanger 38 in the return flow line 33. At the expansion valve 35, a portion of the condensate of 25 bar to about 13.5 bar is expanded, causing the condensate evaporates abruptly and a
- the second return line 33 into the second condensate separator 29 preferably flows into an upper region thereof. In the area of the second condensate separator 29 vapor is thus generated from the condensate in a pressure range between 13-14 bar and at a temperature of about 180-190 0 C.
- a return feed line Connected to the upper region of the second condensate separator 36 is a return feed line, which can be brought into fluid communication via a valve 37 with the live steam line 12.
- a valve 37 When the valve 37 is open, the steam generated from the second condensate 29 in the Main steam network or the live steam power line fed back, the pressure of the steam corresponds approximately to the pressure of the live steam network.
- the tissue paper web (not shown) for drying the used r in the Yankee cylinder 10 condensed water vapor is in the form of, to saturated steam temperature present Brüdenwasser (condensate) via the condensate line 17 from the Yankee cylinder 10 and in a pressure range of between 5-6 bar dissipated.
- the condensate is fed to a first condensate separator 18. There is a first separation between the vapor and liquid phases.
- the liquid water (condensate) 22 collects in the lower region of the first condensate container 18 and is compressed with the valve 27 open via the first return line 25 by the first pump 28 (first pressure stage) to approximately 13.5 bar and conveyed to the second condensate separator 29 , The condensate is then fed via a diffuser 30 into the second condensate separator 29, where once again a separation between vapor and liquid phase takes place.
- the liquid condensate 31, which collects in the lower region of the second Kondensatabscheiders 29 is compressed via the valve 32 by the second pump 34 in the second return line 33 of the pressure prevailing in the second condensate 29 pressure between 13-14 bar to 25 bar and with a temperature of about 18O 0 C in the heat exchanger 38 out.
- the condensate still has a pressure of 25 bar but a significantly higher temperature of about 209 0 C.
- Exhaust air of the hot air hood flows at a temperature of at most 500 0 C through the heat exchanger 38 and thereby heats the condensate from the initial temperature of 18O 0 C to about 209 0 C.
- the expansion device in the form of the expansion valve 35 the pressure level of the heated condensate abruptly from 25 bar to 13.5 bar reduced, which also results in a temperature reduction to saturated steam temperature. By this pressure reduction, the condensate evaporates abruptly, so that the condensate passes into the vapor phase.
- the steam is discharged via the return flow line 33 into the second condensate separator 29 and can be fed back from there via the return feed line 36 when the valve 37 is open into the live steam network.
- the second pressure stage with a pressure increase to 25 bar the boiling temperature of the condensate is markedly increased, so that otherwise any vapor bubbles contained in the condensate are avoided.
- the heat transfer from the exhaust air to the condensate in the heat exchanger 38 can be made more efficient. As a result, a more efficient utilization of the energy content of the exhaust air can be achieved.
- the system according to the invention Due to the system according to the invention, it is possible for a paper machine with a steam consumption of 7-9 tons per hour to recycle 1-3 tons of steam per hour into the live steam network 12. As a result, the actual live steam demand from the grid is reduced by 1-3 tons, which can significantly reduce the costs of live steam (up to 1/3).
- the feedback power in the live steam network from a control engineering point of view is particularly advantageous because there is no need fluctuations.
- the Frischdampfnet z which provides live steam in a quantity of at least 20 tonnes, forms a large buffer and can buffers the jerk-fed 1-3 tons without any control problems. This can lead to any over-supply of the Yankee cylinder with steam and thus to an excessive increase in temperature or fluctuations.
- condensate recovery and vapor recovery can also reduce the amount of condensate that is to be drained through lines 24 and 26 into the condensate collection vessel by 1-3 tons.
- the reduced amount of cooling water also leads to a reduction in production costs.
- the present system represents a significant advantage over the prior art.
- FIG. 2 differs from that in FIG. 1 in that the second pressure stage with the second return line 33 is omitted from the valve 32 and the pump 34 as well as the expansion valve 35 and the heat exchanger 38.
- the condensate 22 is compressed in the first condensate separator 18 via the pump 28 and the first return line 25 to 13 bar and via the diffuser 30 in the second Kondensatabscheider 29th fed.
- the liquid condensate collects in the lower region of the second condensate separator 29.
- the exhaust duct 15 in the form of a pipe heat exchanger (air - water) 39 led, so that the heat of the exhaust air in the exhaust duct 15, via the valve 43 and the conduit 41 flows into the helix 39 and is transferred directly to the condensate 31 contained in the second condensate separator 29 and evaporates it in the second condensate separator.
- the cooler exhaust air is supplied via the blower 16 to the other heat recovery measures already mentioned above.
- the steam generated in the second condensate separator 29 is in turn fed back via the return feed line 36 when the valve 37 is open into the live steam line 12 and thus into the live steam network.
- the advantage of this embodiment is that it is possible to dispense with the second pressure stage and its element, as a result of which the investment costs can possibly be reduced.
- the structure of the device is so much easier constructively.
- a disadvantage of this embodiment over the embodiment in Fig. 1, however, is that the second Kondensatabscheider 29 is provided at the top position, that is directly under or on the hall roof of the machine shop, which receives the paper machine.
- such a container has large outer dimensions and a weight between about 30-50 tons, which can result in structural problems.
- the second embodiment offers the same advantages as those explained with reference to FIG.
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Priority Applications (9)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
CN200980156631.XA CN102317541B (zh) | 2009-02-11 | 2009-12-22 | 使用蒸汽回收干燥棉纸幅面的装置和方法 |
NZ594515A NZ594515A (en) | 2009-02-11 | 2009-12-22 | Device and method for drying a tissue paper web using steam recapture |
CA2750937A CA2750937C (en) | 2009-02-11 | 2009-12-22 | Device and method for drying a tissue paper web using steam recovery |
RU2011137402/12A RU2517803C2 (ru) | 2009-02-11 | 2009-12-22 | Устройство и способ сушки полотна тонкой бумаги с использованием возврата пара |
US13/146,958 US8925217B2 (en) | 2009-02-11 | 2009-12-22 | Device and method for drying a tissue paper web with steam recapture |
AU2009339804A AU2009339804B2 (en) | 2009-02-11 | 2009-12-22 | Device and method for drying a tissue paper web using steam recapture |
ES09801211T ES2397994T3 (es) | 2009-02-11 | 2009-12-22 | Dispositivo y procedimiento para el secado de una banda de papel tisú con recuperación de vapor |
MX2011008424A MX2011008424A (es) | 2009-12-22 | 2009-12-22 | Dispositivo y metodo para secar una cinta continua de papel tisu mediante la utilizacion de recuperacion de vapor. |
EP09801211A EP2396469B1 (de) | 2009-02-11 | 2009-12-22 | Vorrichtung und verfahren zum trocknen einer tissuepapierbahn mit dampfrückgewinnung |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE102009000756.3 | 2009-02-11 | ||
DE102009000756 | 2009-02-11 |
Publications (1)
Publication Number | Publication Date |
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WO2010091765A1 true WO2010091765A1 (de) | 2010-08-19 |
Family
ID=42027723
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/EP2009/067753 WO2010091765A1 (de) | 2009-02-11 | 2009-12-22 | Vorrichtung und verfahren zum trocknen einer tissuepapierbahn mit dampfrückgewinnung |
Country Status (12)
Country | Link |
---|---|
US (1) | US8925217B2 (de) |
EP (1) | EP2396469B1 (de) |
CN (1) | CN102317541B (de) |
AU (1) | AU2009339804B2 (de) |
CA (1) | CA2750937C (de) |
CL (1) | CL2011001964A1 (de) |
CO (1) | CO6420363A2 (de) |
EC (1) | ECSP11011269A (de) |
ES (1) | ES2397994T3 (de) |
NZ (1) | NZ594515A (de) |
RU (1) | RU2517803C2 (de) |
WO (1) | WO2010091765A1 (de) |
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WO2012175461A1 (de) * | 2011-06-20 | 2012-12-27 | Voith Patent Gmbh | Verfahren und system zur wärmerückgewinnung in einer trockenpartie einer maschine zur herstellung einer materialbahn |
WO2012175446A1 (de) * | 2011-06-20 | 2012-12-27 | Voith Patent Gmbh | Verfahren und system zur wärmerückgewinnung für eine trockenpartie einer maschine zur herstellung einer materialbahn |
CN103764908A (zh) * | 2011-06-20 | 2014-04-30 | 沃依特专利有限责任公司 | 用于对制造材料幅面的机器的干燥部回收热量的方法和系统 |
EP2775030A1 (de) | 2013-03-06 | 2014-09-10 | Valmet S.p.A. | Anordnung zum Trocknen einer Tissuepapierbahn und Verfahren zum Zurückgewinnen von Dampf beim Trocknen einer Tissuepapierbahn |
DE102017126372A1 (de) * | 2017-11-10 | 2019-05-16 | Voith Patent Gmbh | Vorrichtung und Verfahren zur Trocknung einer Faserstoffbahn unter Verwendung einer Dampfrückgewinnung |
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GB2622394A (en) * | 2022-09-14 | 2024-03-20 | James Cropper Plc | A steam supply system and a method of supplying steam |
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EP3150761B1 (de) | 2015-09-29 | 2018-12-12 | Voith Patent GmbH | Maschine zur herstellung oder verarbeitung einer faserstoffbahn mit einem dampfbeheizten zylinder und einer vorrichtung zur dampfversorgung des zylinders, und verfahren zur dampfrückgewinnung eines dampfbeheizten zylinders in einer maschine zur herstellung oder verarbeitung einer faserstoffbahn |
DE102016202587A1 (de) | 2015-11-03 | 2016-04-07 | Voith Patent Gmbh | Vorrichtung und Verfahren zur Wärmerückgewinnung |
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 |
US11035259B2 (en) | 2018-03-26 | 2021-06-15 | Daniel W. Sonnek | Method and system for stack heat recovery |
CN111549560B (zh) * | 2020-05-15 | 2021-08-10 | 黄建卫 | 一种可辅助烘缸运行的纸张干燥系统及其辅助方法 |
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- 2009-12-22 EP EP09801211A patent/EP2396469B1/de active Active
- 2009-12-22 NZ NZ594515A patent/NZ594515A/xx unknown
- 2009-12-22 CN CN200980156631.XA patent/CN102317541B/zh active Active
- 2009-12-22 ES ES09801211T patent/ES2397994T3/es active Active
- 2009-12-22 CA CA2750937A patent/CA2750937C/en not_active Expired - Fee Related
- 2009-12-22 WO PCT/EP2009/067753 patent/WO2010091765A1/de active Application Filing
- 2009-12-22 AU AU2009339804A patent/AU2009339804B2/en not_active Ceased
- 2009-12-22 RU RU2011137402/12A patent/RU2517803C2/ru active
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2011
- 2011-08-11 CL CL2011001964A patent/CL2011001964A1/es unknown
- 2011-08-11 EC EC2011011269A patent/ECSP11011269A/es unknown
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Cited By (13)
Publication number | Priority date | Publication date | Assignee | Title |
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WO2011144366A1 (de) * | 2010-05-19 | 2011-11-24 | Voith Patent Gmbh | Verfahren und vorrichtung zur wärmerückgewinnung in einer trockenpartie einer maschine zur herstellung einer faserstoffbahn |
CN103764908B (zh) * | 2011-06-20 | 2017-03-15 | 沃依特专利有限责任公司 | 用于对制造材料幅面的机器的干燥部回收热量的方法和系统 |
WO2012175461A1 (de) * | 2011-06-20 | 2012-12-27 | Voith Patent Gmbh | Verfahren und system zur wärmerückgewinnung in einer trockenpartie einer maschine zur herstellung einer materialbahn |
WO2012175446A1 (de) * | 2011-06-20 | 2012-12-27 | Voith Patent Gmbh | Verfahren und system zur wärmerückgewinnung für eine trockenpartie einer maschine zur herstellung einer materialbahn |
CN103748283A (zh) * | 2011-06-20 | 2014-04-23 | 沃依特专利有限责任公司 | 制造材料幅面的机器的干燥部中回收热量的方法和系统 |
CN103764909A (zh) * | 2011-06-20 | 2014-04-30 | 沃依特专利有限责任公司 | 对制造材料幅面的机器的干燥部回收热量的方法和系统 |
CN103764908A (zh) * | 2011-06-20 | 2014-04-30 | 沃依特专利有限责任公司 | 用于对制造材料幅面的机器的干燥部回收热量的方法和系统 |
EP2775030A1 (de) | 2013-03-06 | 2014-09-10 | Valmet S.p.A. | Anordnung zum Trocknen einer Tissuepapierbahn und Verfahren zum Zurückgewinnen von Dampf beim Trocknen einer Tissuepapierbahn |
WO2014135484A1 (en) * | 2013-03-06 | 2014-09-12 | Valmet S.P.A. | An arrangement for drying a tissue paper web and a method for recapturing steam during drying of a tissue paper web |
DE102017126372A1 (de) * | 2017-11-10 | 2019-05-16 | Voith Patent Gmbh | Vorrichtung und Verfahren zur Trocknung einer Faserstoffbahn unter Verwendung einer Dampfrückgewinnung |
AT521069A3 (de) * | 2018-03-26 | 2020-01-15 | Voith Patent Gmbh | Vorrichtung und Verfahren zur Trocknung einer Faserstoffbahn unter Verwendung einer Dampfrückgewinnung |
AT521069B1 (de) * | 2018-03-26 | 2020-08-15 | Voith Patent Gmbh | Vorrichtung und Verfahren zur Trocknung einer Faserstoffbahn unter Verwendung einer Dampfrückgewinnung |
GB2622394A (en) * | 2022-09-14 | 2024-03-20 | James Cropper Plc | A steam supply system and a method of supplying steam |
Also Published As
Publication number | Publication date |
---|---|
EP2396469A1 (de) | 2011-12-21 |
RU2517803C2 (ru) | 2014-05-27 |
CN102317541B (zh) | 2014-12-03 |
EP2396469B1 (de) | 2012-12-12 |
CA2750937C (en) | 2016-10-18 |
NZ594515A (en) | 2013-01-25 |
US20110277340A1 (en) | 2011-11-17 |
RU2011137402A (ru) | 2013-03-20 |
AU2009339804B2 (en) | 2015-11-26 |
AU2009339804A1 (en) | 2011-09-01 |
CA2750937A1 (en) | 2010-08-19 |
CO6420363A2 (es) | 2012-04-16 |
US8925217B2 (en) | 2015-01-06 |
CL2011001964A1 (es) | 2012-01-20 |
CN102317541A (zh) | 2012-01-11 |
ES2397994T3 (es) | 2013-03-12 |
ECSP11011269A (es) | 2011-09-30 |
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