CA2287355C - Method for optimizing evaporation drying of paper, runnability, and paper quality as well as dryer section that makes use of the method in a paper machine - Google Patents
Method for optimizing evaporation drying of paper, runnability, and paper quality as well as dryer section that makes use of the method in a paper machine Download PDFInfo
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- CA2287355C CA2287355C CA002287355A CA2287355A CA2287355C CA 2287355 C CA2287355 C CA 2287355C CA 002287355 A CA002287355 A CA 002287355A CA 2287355 A CA2287355 A CA 2287355A CA 2287355 C CA2287355 C CA 2287355C
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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
- D21F5/02—Drying on cylinders
- D21F5/04—Drying on cylinders on two or more drying cylinders
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Abstract
A method and an equipment for evaporation drying of a paper web that com es from the press section of a paper machine in three successive stages I, II a nd III carried out in the direction of progress of the web. (I) in the first stage, the pap er web coming from the press section of the paper machine is heated in a short section of the paper machine in the machine direction quickly to a temperature of 55.degree.C to 85.degree.C, and web breaks of the relatively moist and, thus, weak web are minimized; (II) the main evaporation drying of the web is carried out so that the evaporation efficiency and the rate of increase in the dry solids content of the web are substantially high er than in the first stage or in the final stage (III), and the web temperature does substantially not rise while the drying proceeds; (III) in the final stage, the drying is continued with a decreasing evaporation efficiency and with such an average rate of increase in the dry solids content of the web in the machine direction as is lower than in the preceding state (II) but higher than in a conventional cylinder drying with single-wire draw so that the paper quality can be controlled at the same time.
Description
Method for optimizing of evaporation drying of paper, runnability, and of paper quality as well as dryer section that makes use of the method in a paper machine The invention concerns a method for evaporation drying of the paper web that comes from the press section of a paper machine from a dry solids content of lco 35...55 % to a dry solids content of kl ~ 90...98 % .
Also, the invention concerns a dryer section of a paper machine for carrying out the method.
As is known from the prior art, in mufti-cylinder dryers of paper machines, twin-wire draw and/or single-wire draw is/are employed. In twin-wire draw the groups of drying cylinders comprise two wires, which press the web one from above and the other one from below against heated cylinder faces. Between the rows of drying cylinders, which are usually horizontal rows, in twin-wire draw, the web has free and unsupported draws, which are susceptible of fluttering, which may cause web breaks, in particular so in the stages of the drying in which the web is still relatively moist and, therefore, of low strength. This is why, in recent years, ever increasing use has been made of said single-wire draw, in which each group of drying cylinders includes just one drying wire, on whose support the web runs through the whole group so that the drying wire presses the web on the drying cylinders against the heated cylinder faces, whereas on the reversing cylinders or rolls between the drying cylinders the web remains at the side of the outside curve. Thus, in single-wire draw, the drying cylinders are placed outside the wire loop, and the reversing cylinders or rolls inside said loop. From the prior art, dryer sections are known that comprise so-called normal groups with single-wire draw only, in which the drying cylinders are placed in the upper row and the reversing cylinders or rolls are in the lower row.
Also, the invention concerns a dryer section of a paper machine for carrying out the method.
As is known from the prior art, in mufti-cylinder dryers of paper machines, twin-wire draw and/or single-wire draw is/are employed. In twin-wire draw the groups of drying cylinders comprise two wires, which press the web one from above and the other one from below against heated cylinder faces. Between the rows of drying cylinders, which are usually horizontal rows, in twin-wire draw, the web has free and unsupported draws, which are susceptible of fluttering, which may cause web breaks, in particular so in the stages of the drying in which the web is still relatively moist and, therefore, of low strength. This is why, in recent years, ever increasing use has been made of said single-wire draw, in which each group of drying cylinders includes just one drying wire, on whose support the web runs through the whole group so that the drying wire presses the web on the drying cylinders against the heated cylinder faces, whereas on the reversing cylinders or rolls between the drying cylinders the web remains at the side of the outside curve. Thus, in single-wire draw, the drying cylinders are placed outside the wire loop, and the reversing cylinders or rolls inside said loop. From the prior art, dryer sections are known that comprise so-called normal groups with single-wire draw only, in which the drying cylinders are placed in the upper row and the reversing cylinders or rolls are in the lower row.
The highest web speeds in paper machine are to-day up to an order of 25 metres per second and slightly higher, taut before long the speed range of 25...40 metres per second will be taken to common use. In such a case, a bottleneck for the runnability of a paper machine will be the dryer section, whose length with the prior-art multicylinder dryers would also become intolerably long. If it is imagined that a present day multi-cylinder dryer were used in a newsprint machine at a web speed of 40 mps, it would include about 70 drying cylinder (ra ~ 1800 mm), and its length in the machine direction would be ~ 180 metres. In such a case, the dryer section would comprise about separate wire groups and a corresponding number of draws over group gaps. It is probable that, in a speed range of 30...40 mps, the runnability of normal prior-art mufti-cylinder dryers is no longer even nearly satisfactory, but web breaks would occur abundantly, lowering the efficiency of the paper machine.
In a speed range of 30...40 mps and at higher speeds, the prior-art mufti-cylinder dryers would also become uneconomical, because the cost of investment of an excessively long paper machine hall would become unreasonably high. It can be estimated that the cost of a paper machine hall is at present typically about 1 million FIM per metre in the machine direction.
It is known from the prior art to use various impingement-drying/through-drying units for evaporation drying of a paper web, which units have been employed in particular in the drying of a tissue paper. With respect to this prior art, reference is made, by way of example, to the following patf,nt literature: US-A-3,301,746, US-A-3,418,723, US-A-3,447,247, US-A-3,541,697, US-A-3,956,832, US-A-4,033,048, CA-A-2,061,976, DE-A-2,212,209, DE-A-2,364,346, EP-A2-0,427,218, FI-B-57,457 (equivalent to SE-C-7503134-4), FI-B-87,669, and :FI-A-931263 (equivalent to EP-0,620,313-A1).
The present invention is, in connection with increasing of paper machine speeds and with modernizations, directed towards permitting fitting of a new dryer section in the place of an existing mufti-cylinder dryer. In relation to this, present invention is directed towards the provision of a dryer section concept that permits ever shorter dryer sections compared with the prior-art dryer sections.
The present invention is further directed towards making it possible to provide a dryer section concept in which difff;rent evaporation devices and techniques can be applied optimally in the different stages of drying so that a short construction of the dryer section, a good quality of the paper and a runnability sufficiently free from disturbance are achieved.
The invention is principally directed towards the provision of a novel module for a paper web and dryer sections that make use of said module/modules, which are suitable for use at high web speeds of v > 25 metres per second, which speed can be up to an order of v ~ 30...40 metres per second or even higher.
The present invention further is directed towards increasing the drying capacity by means of impingement drying and/or through-drying and in this way to make the length of the dryer section shorter, v~rhich contributes to an improvement of the runnability of the dryer section.
The invention additionally is directed towards providing such a drying method and drying equipment by whose means, in said high speed range, the length of the dryer section in the machine direction can, nevertheless, become reasonable so that its length does not, at least not substantially, exceed the length of the cylinder dryers currently in operation. An achievement of this objective would permit renewals and modernizations of paper machines in existing paper machine hall up to, and even beyond, a web speed of v ~ 40 metres per second.
The present invention further is directed towards the provision of a drying method and a dryer section that applies said method wherein the web is reliably affixed to the drying wire over the entire length of the dryer section so that cross-direction shrinkage of the web can be substantially prevented.
The present invention further is directed towards the provision of a drying method and a dryer section that applies said method wherein the web is prevented from sticking to the cylinders in the initial end of the dryer section and to improve both the paper quality and the runnability of the paper machine.
In a speed range of 30...40 mps and at higher speeds, the prior-art mufti-cylinder dryers would also become uneconomical, because the cost of investment of an excessively long paper machine hall would become unreasonably high. It can be estimated that the cost of a paper machine hall is at present typically about 1 million FIM per metre in the machine direction.
It is known from the prior art to use various impingement-drying/through-drying units for evaporation drying of a paper web, which units have been employed in particular in the drying of a tissue paper. With respect to this prior art, reference is made, by way of example, to the following patf,nt literature: US-A-3,301,746, US-A-3,418,723, US-A-3,447,247, US-A-3,541,697, US-A-3,956,832, US-A-4,033,048, CA-A-2,061,976, DE-A-2,212,209, DE-A-2,364,346, EP-A2-0,427,218, FI-B-57,457 (equivalent to SE-C-7503134-4), FI-B-87,669, and :FI-A-931263 (equivalent to EP-0,620,313-A1).
The present invention is, in connection with increasing of paper machine speeds and with modernizations, directed towards permitting fitting of a new dryer section in the place of an existing mufti-cylinder dryer. In relation to this, present invention is directed towards the provision of a dryer section concept that permits ever shorter dryer sections compared with the prior-art dryer sections.
The present invention is further directed towards making it possible to provide a dryer section concept in which difff;rent evaporation devices and techniques can be applied optimally in the different stages of drying so that a short construction of the dryer section, a good quality of the paper and a runnability sufficiently free from disturbance are achieved.
The invention is principally directed towards the provision of a novel module for a paper web and dryer sections that make use of said module/modules, which are suitable for use at high web speeds of v > 25 metres per second, which speed can be up to an order of v ~ 30...40 metres per second or even higher.
The present invention further is directed towards increasing the drying capacity by means of impingement drying and/or through-drying and in this way to make the length of the dryer section shorter, v~rhich contributes to an improvement of the runnability of the dryer section.
The invention additionally is directed towards providing such a drying method and drying equipment by whose means, in said high speed range, the length of the dryer section in the machine direction can, nevertheless, become reasonable so that its length does not, at least not substantially, exceed the length of the cylinder dryers currently in operation. An achievement of this objective would permit renewals and modernizations of paper machines in existing paper machine hall up to, and even beyond, a web speed of v ~ 40 metres per second.
The present invention further is directed towards the provision of a drying method and a dryer section that applies said method wherein the web is reliably affixed to the drying wire over the entire length of the dryer section so that cross-direction shrinkage of the web can be substantially prevented.
The present invention further is directed towards the provision of a drying method and a dryer section that applies said method wherein the web is prevented from sticking to the cylinders in the initial end of the dryer section and to improve both the paper quality and the runnability of the paper machine.
With respect to the prior art most closely related to the present invention, reference is made to the applicant's FI Patent 93,876 (equivalent to US-pat 5,553,393) in which a dryer section of a paper machine is described which is composed of cylinder groups with single-wire draw and in which dryer section it is considered novel that, in view of optimizing the drying capacity calculated per unit of length of the dryer section in the machine direction, as the drying makes progress, different ratios k = D/d of the drying-cylinder diameter D to the reversing-roll diameter d are employed, so that, in the first group or groups in the initial end of the dryer section, said ratio k = kl is higher than the ratio k = kz in the groups in the middle area of the dryer section, kl >
k2 and that in the group or groups in the final and of the dryer section, a diameter ratio k3 is used that is higher than said ratio k2, k3 > k2. In said FI patent an effort has been made to choose the diameter ratio D/d of drying cylinder to reversing roll optimally taking into account the different evaporation curves that are carried into effect in different areas of the dryer section. In said FI patent, in the initial end of the dryer section, preferably in one group, said diameter ratio D/dl that is used is higher than average, compared with the middle area of the dryer section, for example in the second, third and fourth wire groups. The last mentioned wire groups are in the area where the main evaporation of water takes place from the web. Said higher diameter ratio D/d is also employed in the final end of the dryer section, in which a significant proportion of the evaporation takes place on the curve sector of the; wire and the web on the drying cylinders.
In said FI patent, owing to the; optimally chosen and varied diameter ratio k = D/d of drying cylinder to reversing roll, the length of the drying section is estimated to be shortened, at the maximum, by about 10 per cent in comparison with a situation in which said ratio k is used as invariable over the entire length of the dryer section. It has been understood in said FI patent that, as the drying proceeds, the nature of the drying process will change substantially. However, only the diameter ratio of the drying cylinder to the reversing roll, k = D/d, has been varied in order to optimize the drying, which does, hawever, not take; it far enough from the point of view of optimizing the drying process and the drying configuration, especially since the speed of paper machines become higher and the quality requirements imposed on the paper become ever stricter.
The present invention is direr;ted towards the further development of the evaporation drying and the dryer sections in paper machines so that the drying process in different parts of the drying section, in different phases of the drying process, and the dryer S section configuration can be optimized and the length of the dryer section shortened of kept unchanged while the speed become higher.
The invention additionally is .directed towards optimizing the runnability of the paper machine in different phases of the drying procedure so that the efficiency of the paper machine is improved while breaks are fewer and towards taking advantage of the different structures/methods/processes in the different phases of the paper drying process so that the quality properties of the paper can be optimized.
The nature of the drying procedures has been clarified further in the applicant's recent research and in dryer section that are in operation and in test runs on a test device. The invention is partly based on thc: observation that in the dryer section of a paper machine the drying process can be divided into three process stages that are different from each other:
(I) heating stage, in which evaporation does not take place to a substantial extent, but the water present in the web is mainly heated, (II) main evaporation area, in which the rate of evaporation remains substantially invariable when cylinder drying alone is used and in which the main evaporation of water from between the fibres and from their surface takes place, and (III) final evaporation area, in which the rate of evaporation becomes lower and the proportion of the evaporation that takes place on the drying cylinder is increased, and in this stage mainly evaporation of water present inside the fibres takes place.
It has also been a problem in the prior-art mufti-cylinder dryers that in said first stage (I) it has not been possible to use a temperature high enough in view of optimizing the drying, because, when the paper web is in direct contact with the hot faces on the drying cylinders, at temperatures higher than a certain figure, sticking of the web to the hot surface of the cylinder occurs, from which web breaks and standstill follow. It has been noticed that excessively hat contact drying cylinders also have detrimental effects on the quality properties of the paper.
The present invention is further directed towards the further development of said prior art, elimination of drawbacks of the prior art that were mentioned above and of those that will come out later, and implementation of other objectives of the invention.
In accordance with one aspect of the present invention, there is provided a method for evaporation drying a paper web having a dry solids content from about 35% to about 55% until the web has a dry solids content from about 90% to about 98%
comprising the steps of passing the web through three successive stages in a running direction of the web as follows:
in the first stage, passing the web through a short section in the machine direction and rapidly heating the web in the short section to a temperature from about 55° C. to about 85° C., in the second stage, drying the web utilizing an evaporation efficiency and rate of increase in dry solids content per unit of length of the dryer section in the machine direction which are higher than in the first stage or in the third stage and such that the temperature of the web does not rise substantially in the second stage, and in the third stage, continuing dying of the web with a decreasing evaporation efficiency and an average rate of increase in the dry solids content of the web in the machine direction which is lower than the rate of increase in the dry solids content of the web in the second stage.
The method aspect of the invention, therefore, is mainly characterized in that the method consists of three successive stages I, II and III, that are carried out in the direction of progress of the web in the sequence given as follows:
I in the first stage, the paper web coming from the press section of the paper machine is heated in a short section of the paper machine in the machine direction quickly to a temperature of 55° to 85° C, preferably to a temperature of about 70° C, and in this section the web i:c passed so that web breaks of the relatively moist and, thus, weak web are minimized, II after the first stage I, in this second stage II the main evaporation drying of the web is earned out with such m evaporation efficiency and rate of increase in dry solids content per unit of length o:f the dryer section in the machine direction that said evaporation efficiency and rate of increase in dry solids content of the web are substantially higher than in the first stage or in the final stage III, and the web temperature does substantially not rise in the second stage while the drying proceeds, III in the third and final stage, the drying is continued with a decreasing evaporation efficiency and with such an average rate of increase in the dry solids content of the web in the machine direction as is lower than in the preceding stage II
but higher than in a conventional cylinder drying with single-wire draw so that the paper quality can be controlled at the same time.
In accordance with another aspect of the present invention, there is provided a dryer section of a paper machine, comprising a first drying wire unit arranged to receive a web from a press section preceding the dryer section, said first drying unit comprising at least one of blow boxes and radiation dryer units for heating the web in a first stage without contacting the web, the web being passed in said first drying unit through a short section in the machine direction and rapidly heated in the short section to a temperature from about SS° C.. to about 85 ° C., and additional dryer units arranged after said first drying unit in the running direction of the web, said additional dryer units comprising at least one group with single-wire draw including contact drying cylinders arranged in a first row and reversing suction cylinders arranged in a second row below said first row of contact drying cylinders, a first set of said additional drier units being arranged to evaporation dry the web in a second stage utilizing an evaporation efficiency and rate of increase in dry solids content per unit of length of the dryer section in the machine direction which are higher than in the first stage and such that the temperature of the web does not rise substantially in the second stage, and g a second set of said additional dryer units arranged after said first set of additional dryer units and being arranged to continue drying the web in a third stage with a decreasing evaporation efficiency and an average rate of increasing in the dry solids content of the web in the machine direction which is lower than the rate of increase in the dry solids content of the web in the second stage.
A dryer section in accordance; with the aspect of the invention is mainly characterized in that, after the press section of the paper machine, the dryer section comprises the following dryer units that are placed in the given sequence in the machine direction:
in order to carry out the first si:age I of the method, the first unit is a drying wire unit in which the paper web runs past blow boxes and/or radiation dryer units, by whose means the web is heated without a direct contact with heated faces, in order to carry out the second stage II of the method, dryer units that comprise at least one single-wire group with single-wire draw that is open towards the bottom, in which the contact drying cylinders are in the upper row and the reversing suction cylinders are in the lower row so that removal of broke can take place downwards by the effect of gravity.
In the first stage I in the method in accordance with the invention, such a construction of the dryer section is used as also has optimal runnability properties so that in this stage, when the web is still moist and relatively weak, web breaks can be minimized.
The final stage III of the method of the invention is earned out with such solutions of equipment as also permit control of quality properties of paper, such as brightness, curl, etc.
With the method in accordance with the present invention and with a dryer section concept that carnes out the method it is possible to achieve the objectives mentioned above and to eliminate said drawbacks substantially. In accordance with the invention it is possible to provide a dryer section that is shorter and more compact than in the prior art also at high machine speeds so that the operating quality of the dryer section still remains good.
In the method and the dryer section in accordance with the invention the web is preferably dried so that in the first stage I the drying energy is at least mainly applied from the side of and through the upper surface of the web, in the second stage II the drying energy is applied to the; web from the side of and through its lower surface, and in the third stage III the drying energy is applied to the web from and through its both surfaces.
In the following, the invention will be described in detail with reference to some exemplifying embodiments of the invention illustrated in the figures in the accompanying drawings, the invention being by no means strictly confined to the details of said embodiments, wherein:
Figure lA is a schematic side view of a dryer section in accordance with the invention in which the method in accordance with the invention can be applied favourably;
Figure 1 B shows a preferred ~contact-drying/impingement-drying unit used in a dryer section in accordance with the invention, of which units there are three in the dryer section shown in Fig. 1, separated from one another by single-wire groups;
Figure 1 C shows the last wire group of the dryer section in a scale larger than Fig. 1 A, in which group the stage III of the method in accordance with the invention is earned out;
Figure 2 is a graphic illustration of the different stages of the method in accordance with the invention in a system of coordinates of dry solids content of the web - length of the dryer section in the machine direction, compared with a prior-art multicylinder dryer;
Figure 3 is a graphic illustration similar to Fig. 2 of the dryer method in accordance with the invention and of prior-art drying method in a system of coordinates o evaporation capacity - length of the dryer section in the machine direction;
Figure 4 is an illustration similar to Figs. 2 and 3 of the distribution of paper web temperature in the machine direction of the dryer section; and Figure 5 illustrates the evaporation capacity of stage III in accordance with the invention as a function of the: dry solids content percentage of the web in the method in accordance with the invention and in prior-art dryer section.
In the drawings, Figure lA shows a particularly favourable overall concept of a dryer section in accordance with the invention. As is shown in Fig. lA, the paper web W is passed from the press section 10 of the paper machine at a dry solids content of lco 35...55 % and at a temperature of To ~ 30...60°C on the bottom face of the transfer fabric 11 and supported by a PressRunTM box l la onto the top face of the drying wire 12 over its guide roll 13. The first planar drying unit R~ comprises a blow hood 15, under which the web W to be dried runs on the horizontal run of the wire 12, which is supported by the rolls 14. Said horizontal run of the wire 12 forms a plane consisting of grooved rolls and/or of suction boxes or blow boxes to support the web W.
In the unit Rl, an intensive drying energy impulse is applied to the web W in which connection, after the unit Rl, the temperature of the web W is Tl ~
60...85°C. In the unit Rl, primarily heating of the web W and of the water con-tained in it takes place, but no substantial evaporation of water as yet. The length L1 of the unit R1 in the machine direction is typically of an order of L1 .=
3...10 m.
In the unit R1, the paper web runs on support of the upper run of the drying wire 12 5 along a linear path in the horizontal plane so that it has no major changes in the direction and that, thus, no high dynamic forces are applied to it which might produce a web break in the web, which is still relatively moist and, thus, of low strength. In the interior of the blow hood 15, there is a nozzle arrangement, by whose means hot drying gases, such as air or steam, are blown against the top face 10 of the web. Additionally or alternatively, it is possible to employ infrared heaters.
Said blow devices and/or radiators in the unit Ri can be arranged so that their output in the cross direction of the web W is adjustable so as to provide profiling of the web W in the cross direction.
In Fig. lA, the unit R1 is followed by the first so-called normal (not inverted) single-wire unit R2, onto whose drying wire 22 the web W is transferred as a closed draw in the area of the first reversing suction roll 21. The single-wire unit R2, and so also the subsequent single-wire units R4, R6 and Rg that are open towards the bottom comprise steam-heated contact-drying cylinders 20 fitted in the upper row and reversing suction rolls 21 fitted in the lower row, for example the applicant's said YAC-rolls'. Below the cylinders 20, there are doctors and ventilation blow devices 25. The paper web W to be dried enters into direct contact with the faces of the steam-heated drying cylinders 20, and on the reversing suction rolls 21 the web W remains on the drying wire 22 at the side of the outside curve.
In Fig. lA, after the group R2 with single-wire draw, there follows a drying unit R3 in accordance with the invention, which, in accordance with Fig. 1B, comprises two contact-drying cylinders 30 and a large-diameter D1 impingement-drying/through-drying cylinder 31 with a perforated mantle, which cylinder will be called a large cylinder in the following. Around the contact-drying cylinders 30 and around the large cylinder 31, a drying wire 32 is fitted to run, which wire is guided by the guide rolls 33. The impingement-drying/through-drying hood module M1 of the _ T _ __. _~ _. __ _ _... ~ _ drying unit R3 is fitted in the basement space KT underneath the floor level of the paper machine hall on support of the floor level K2-K2 of said space.
The central axes of the contact-drying cylinders 30 in the unit R3 and in the correspon-ding following drying units RS and R7 in accordance with the present invention are placed substantially in the floor plane of the paper machine hall or in the vicinity of said plane K1-K1, preferably slightly above said plane. The paper web W to be dried is passed from the single-wire unit R2 as a closed draw onto the first drying cylinder 30 in the drying unit R3 (Rn), after which the web W is passed on the wire 32 of the unit R3 over the large cylinder 31 of the first module Ml on a remarkably large sector b .= 220...280° on support of the drying wire 32 and further onto the second drying cylinder 30 in the unit R3 (Rn). From this drying cylinder 30 the web W is transferred as a closed draw into the next normal unit R4 with single-wire draw, which unit is substantially similar to the unit R2 described above.
After this, there follows the second drying unit RS (Rn), which unit is similar to the drying unit R3 described above and whose large cylinder 31 is also placed in the basement space KT. After the drying unit Rg the web W is passed as a closed draw into the next single-wire unit R6, which is followed by the third drying unit R7 (Rn), whose large cylinder 31 is likewise placed in the basement space KT. The unit R7 is followed by a particular single-wire unit Rg, from which the web W°uc is passed to the reel-up or into a finishing unit (not shown). The construction and operation of the particular unit Rg will be described in more detail later with reference to Fig. 1C.
In the basement space, besides the modules M1, M2 and M3, Fig. lA also shows the pulpers 40a and 40b, between which there is the broke conveyor 41, which carries the paper broke into the pulper 40a and/or 40b. In the event of a web break, the web W can be passed after the unit R1 directly into the pulper 40a placed underneath.
The single-wire units R4, It6, and Rg are open towards the bottom, and therefore the paper broke falls from them by the effect of gravity onto the broke conveyor placed underneath or directly into the pulpers 40a,40b. Also the modules M1, and M3 are open or operable towards the bottom so that the paper broke falls out of connection with them, substantially by the effect of gravity, without major manual operations, onto the broke conveyor 41 placed underneath.
Underneath the modules M i , M2 and M3, above the floor level K2-K2 of the basement space KT, there is still space KTo for various devices, such as ducts through which the heating medium, such as heated air or steam, is passed into the interior of the hoods 35 of the modules M 1, M2 and M3 . Said lower space KT~
is defined from below by the floor level K2-K2 of the basement space and from above by the partition wall 42 placed below the broke conveyor 41. On the drying units R2...Rg there is an air-conditioned hood 50 in itself known.
Figure 1B is a more detailed illustration of the impingement-drying/through-drying hood module M in accordance with the invention. As is shown in Fig. IB, the wire 32a which runs around the large cylinder 31 is first passed around the last lower cylinder 21a in the preceding group Rn_1 with single-wire draw onto the first contact-drying cylinder 30 in the unit Rn, from it further as a short straight run over the sector b = 220 . . . 280 ° of the large cylinder 31 onto the second contact-drying cylinder 30 in the group Rn and over said cylinder on a sector of about 90°. After this the web W follows the face of the cylinder 10 and is transferred as a closed draw onto the drying wire 22 of the next group Rn+ 1. The hood of the large cylinder 3i, which consists of two parts 35, covers the cylinder substantially over the entire curve sector b of the wire 32a and the web W. On the sector b the web W
remains on the wire 32a at the side of the outside curve, so that its outer face is free. The large cylinder 31 is mounted on its axle journals 36, through which a communication is arranged with vacuum devices (not shown), by whose intermediate a suitable vacuum is produced in the interior of the cylinder 31, which vacuum is of an order of p~ ~ 1. ..3 kPa. This vacuum p~ keeps the web W on the wire 32a when the web W is at the side of the outside curve, and, at the same time, the vacuum p0 also promotes possible through-drying taking place through the web W and the wire 32a. The sector 360°-b that remains outside the sector b on the large cylinder 31 is covered by a cover plate 34 placed in the gap between the drying cylinders 30, and so also the last cylinder 21a in the group Rn, which can also be called the reversing cylinder of the group Rn, is covered by an obstacle plate 29. As to its more detailed embodiment, the perforated and grooved outer mantle 31a of the large cylinder is, for example, similar to that described in said FI Pat. Appl. 931263 and illustrated r _....____~ _____. _ _.__-~ 1 above all in Fig. 11 of said patent application, so that the construction will not be described again in this connection.
In accordance with figure 1B, the large cylinder 31 is mounted by means of its axle journals 36 on support of the frame construction 37. In this frame construction, both at the driving side and at the tending side, there are horizontal and machine direction beams 37a, on whose top face, or on rails provided on said top face, the hood halves 35 are arranged to be movable on wheels 39, which hood halves are illustrated in the open position 35a, in which the module M can be serviced. The hood halves 35 are displaced into the open and closed positions by actuating cylinders 38. The module M and its hood 35 are open towards the bottom, so that broke can be removed in the direction of the arrows WA substantially by the effect of gravity onto the broke conveyor 41 placed underneath without substantial manual operations. The top face of the hood 35 has been shaped as smoothly downwards inclined so as to improve the removal of broke.
Further, in the open position 35a of the hood 35, the module M can also be serviced and cleaned easily in other respects. The diameter D1 of the large cylinder 31 is, as a rule, chosen in the range of D 1 > 2 m, as a rule in the range of D 1 .= 2.
. . 8 m, preferably D1 = 2...4 m. The diameter D2 of the drying cylinders 30 in the group Rn is, as a rule, chosen in the range of D2 ~ 1.5...2.5 m, preferably in the range of D2 = 1.8...2.2 m. In the groups Rn_~ and Rn+1 with single-wire draw, the diameter of the drying cylinders 20 is preferably = D2. The diameter D3 of the reversing suction cylinders 21,21a is, as a rule, chosen in the range of D3 =
0.6...1.8 m, preferably D3 = 1Ø..1.5 m. The top face of the hood 35 has been shaped as smoothly downwards inclined to improve the removal of broke.
The wire 32a guide roll 33a placed above the latter drying cylinder 30 can be stationary or displaceable. Between the groups Rn_1, Rn and Rn+1 a little difference in speed can be employed, which is, typically, about 0.1..Ø2 %, so that, on the wires 22,32a,22, the speed becomes higher when the web W moves forwards. In the final end of the dryer section, the difference in speed can also be reversed.
The more detailed construction of the hood 35 of the module M and the circulation arrangements of the drying gases that are blown through it are described in detail in the FI Patent Application No. (971713) to be filed on the same day with the present application by the applicant, especially in its Fig. 3 and the related specification part, to which reference is made in this connection.
Fig. 1C shows, in a larger scale than Fig. lA, the last group Rg with single-wire draw in the dryer section in accordance with the invention, in which group the third stage of the invention is carried out. The paper web W to be dried is brought into the group R8 from the last contact-drying cylinder 30 of the module M3 shown in Fig. lA as a closed draw onto the first reversing suction roll 61 of the group Rg.
There are five of these reversing suction cylinders inside the wire loop 62 in the group Rg. The group Rg includes five contact drying cylinders 60,60A. Two middle ones 60A of these cylinders are contact drying cylinders whose diameter, which is larger than that of the other cylinders 60, is D4 .= 1.8...2.5 m, whereas the diam-eter of the smaller cylinders 60 is DS = 1Ø..1.8 m, and the diameter of the reversing suction cylinders 61 is D6 = 1Ø..1.5 m. Between the reversing suction cylinders 61 there are blowing devices 65 to ventilate the spaces between the cylinders 60,60A and 61 and to promote the drying. There is a blow box 64 above the upper sectors of the reversing suction cylinders 61 free from the web W
and from the wire 62, which promotes maintenance of the vacuum inside cylinders 61.
In order that it should be possible to carry out the stage III of the method in accord-ance with the invention and to achieve a sufficiently high evaporation capacity and an increase in the web W temperature Tw in accordance with the curve TI of Fig. 4 by means of the group Rg shown in Fig. 1C, a drying effect is applied to the web W
by means of contact drying cylinders 60A with large diameter also from the top face of the web W, i.e. from the drying wire 62. For this purpose ventilation hoods are provided above the cylinders 60A, into which hoods sufficiently hot and dry drying air gases are passed through the intake pipe 67. Out of the pressurized interior of the ventilation hoods 66, the humidified ventilation air is discharged into the hood 50 around the dryer section, from where it is removed in a way known T ___.___~~~__ _____.. . ._. _._...__ .___._~_ ~.._ .
from the prior art. These drying gases are blown against the drying wire 62 in the sector d of the cylinders 60A, said sector being preferably d = 180° or even larger.
Thus, evaporation of water is promoted through the upper face of the web W
through the wire 62. The ventilation hoods 66 are shown in their open position 66a, 5 as well as their air intake pipes are shown in their open position 67a. In this position 66a it is possible to clean and service the ventilation hoods, and the web W
thread-ing is also carried out most favourably then. In respect of their construction the ventilation hoods 66 can be similar to those that are described in more detail in the FI Patent Application (971713) to be filed on the same day with the present applica-10 lion.
In respect of the various details of the construction and the Qperation of the ventila-lion hoods 66, reference is made to the prior art coming out from the applicant's FI
Patent Application 951746 and from the FI Patent 83, 679 of Teollisuusmittaus Oy.
Fig. 2 shows the development of the dry solids content KA of the paper over the length L of the dryer section in the machine direction as a function. The curve K
represents an optimized method in accordance with the invention, and the curve KpA
represents the development of the dry solids content with a method and a dryer section of prior art. The curves K and Kpp have been obtained by means of com-puter simulation using the applicant's dryer section process model. The basis for the curve KpA is the applicant's prior-art SymRunT" dryer section concept, which consists of N pcs. of successive groups with single-wire draw that are open towards the bottom, and the curve K is based on a dryer section concept in accordance with Fig. 1.
It can be noticed immediately from Fig. 2 that it has been possible to shorten the length of the dryer section from the length LpA to the length LI, i.e. in practice by about 15...40 percent. In accordance with Figs. 1...4 the method in accordance with the invention is divided into three different stages I, II and III. As is seen in Fig. 2, in the first stage I the rate of increase in dry solids content KA of the web W
becomes higher from the initial value Kp more steeply in accordance with the curve K, in comparison with the curve KpA, because the initial temperature of the web W
is higher, which becomes clear from a comparison of the temperature curves TI
and TpA of the stage I in the figure. Also, in the first stage I, as is shown in Fig. 3, the evaporation efficiency PE is, in accordance with the curve PEI, substantially higher than in the prior-art method, curve PEpA of stage I (Fig. 3). In the invention the first phase I is carried out on a horizontal dryer unit R1 where the web W tem-perature Tw is raised to about 55...85°C, preferably to about 70°C, as comes out from Fig. 4. In the invention this raising of the temperature can be carried out very quickly, because in the unit RI a highly energy-intensive impingement stage and/or infra radiation can be used, because heating of the web W takes place free of contact so that there is no risk of sticking.
Stage II, shown in Figs. 1...4, is the main evaporation area where, in accordance with Fig. 2, the dry solids content KA of the web increases more steeply than in stage I as the drying proceeds. Fig. 3 shows the three successive evaporation peaks PEI, PF.z and PE3 of stage II, at which the maximal evaporation efficiency PE
is of an order of PE ~ 60 kg/m2/h (kilograms per square meter in an hour). These evaporation peaks are achieved by the hood modules M1, M2 and M3 in the dryer section shown in Fig. 1. Depending on the mode of operation of the modules M1, M2 and M3 or equivalent, the maximal evaporation efficiency can be even higher.
Between said peaks PE1, PE2 and PE3, the evaporation efficiency PE is of an order 20 kg/m2/h, i.e. of the same order of magnitude as the evaporation efficiency in accordance with the curve PEpA in Fig. 3 on the average.
In the exemplifying embodyment of Fig. 4, the web temperature TW stays substan-tially invariable in the stage II in accordance with the curves TI and TpA in a range of about 60...70°C. As was stated, the stage II is the main evaporation area where the water is evaporated from between the fibres in the web W and from the fibre surfaces.
In the third stage III in accordance with the invention, the steepness of the increase in the dry solids content decreases in comparison with stage II. The evaporation effi-_ T. ~
__.. . . ._ _ _. . _~ _ _ ciency also decreases in accordance with Fig. 3, whereas the web W temperature TW starts rising from about 70°C to 100...110°C. In the corresponding location in the dryer section in the machine direction, in prior-art methods, the evaporation effi-ciency still remains invariable, in accordance with the curve PEpp in Fig. 3, and so S also the temperature in accordance with the curve TpA in Fig. 4. In the dryer section in accordance with the invention, the stage III is carried out in the last cylinder group Rg, where the evaporation is made more intensive by means of the hoods that are placed above the cylinders 60 A with large diameter, in which hoods suffi-ciently powerful and hot drying gases are applied to the web W placed under the drying wire 62 and to the environment of the wire 62, so that the web W
tempera-ture TW can be raised very steeply in the stage III, in accordance with Fig.
4, in which connection also the water present inside the fibres in the paper web W
can be efficiently evaporated on a sufficiently short length L of the dryer section in the machine direction. Fig. 5 illustrates the evaporation efficiency PE in the stage III of the invention, i.e. the dry solids content KA in the area KA 80...98 %. The curve PRI represents the method in accordance with the invention, and the curve PEpA
a corresponding curve carried out by means of the prior-art SymRun'~ concept.
Fig. 5 shows that in the beginning of the stage III, in accordance with the curve PEI, in the dry solids content area 80.. .82 the evaporation efficiency is substantially higher than in the prior-art concept and somewhat higher than in the dry solids content area 84...91 and in the dry solids content area 93...98. This improvement has mainly been carried out in the particular group Rg by means of the drying cylinders with large diameter and by means of the blowings from their ventilation hoods 66.
Thus, in the drying method and in the dryer section in accordance with the inven-tion, the ultimate dry solids content of the web W, kl = 96...98 % , is achieved in the machine direction length LI of the dryer section, whereas in the prior art a substantially longer length LpA was needed.
As comes out from the above and especially from Fig. lA, the method stage I in accordance with the invention is carried out by applying drying energy mainly through the upper face of the web W. As is shown in Fig. 1, in the second stage II
of the method, drying energy is applied to the web mainly through the lower face of the web only by means of the wire groups Rg, R4, R5, R6, R~ and Rg and by means of the hood modules M1, M2 and M3, whereas in the group Rg (Fig. 1C) and in the stage III drying energy is applied to the web W through its both faces by applying drying energy through the lower face of the web W by means of the contact drying cylinders 60 and 60A and through the upper face of the web by means of the ventilation hoods 66 on the sectors d of the cylinders. This arrangement provides a short dryer section in which, at the same time, it is possible to control the paper quality, for example its curl.
In this context it should be emphasized that the method in accordance with the invention can also be carried out with many other dryer section concepts and solutions of equipment besides those of Figs. lA and 1B. Examples of these other dryer section concepts are some dryer section concepts described in the applicant's FI Patent Applications Nos. (971713 and 971715) to be filed on the same day with the present application. It is an essential feature of the dryer section in accordance with the invention that in said different drying stages I, II and III exactly a sort of a solution of equipment is used in which it is possible to carry out heating of the web and evaporation in accordance with the invention optimally. This inevitably has the consequence that, unlike the prior-art, in the different stages I, II and III of the invention, solutions of equipment different from one another have to be used, which is illustrated in Fig. 1.
In the following, the patent claims will be given, and the various details of the invention can show variation within the scope of the inventive idea defined in said claims and differ from the details described above by way of example only.
T.. T
__-_- ,~__.~.~____ ____ ..__..._ _.._
k2 and that in the group or groups in the final and of the dryer section, a diameter ratio k3 is used that is higher than said ratio k2, k3 > k2. In said FI patent an effort has been made to choose the diameter ratio D/d of drying cylinder to reversing roll optimally taking into account the different evaporation curves that are carried into effect in different areas of the dryer section. In said FI patent, in the initial end of the dryer section, preferably in one group, said diameter ratio D/dl that is used is higher than average, compared with the middle area of the dryer section, for example in the second, third and fourth wire groups. The last mentioned wire groups are in the area where the main evaporation of water takes place from the web. Said higher diameter ratio D/d is also employed in the final end of the dryer section, in which a significant proportion of the evaporation takes place on the curve sector of the; wire and the web on the drying cylinders.
In said FI patent, owing to the; optimally chosen and varied diameter ratio k = D/d of drying cylinder to reversing roll, the length of the drying section is estimated to be shortened, at the maximum, by about 10 per cent in comparison with a situation in which said ratio k is used as invariable over the entire length of the dryer section. It has been understood in said FI patent that, as the drying proceeds, the nature of the drying process will change substantially. However, only the diameter ratio of the drying cylinder to the reversing roll, k = D/d, has been varied in order to optimize the drying, which does, hawever, not take; it far enough from the point of view of optimizing the drying process and the drying configuration, especially since the speed of paper machines become higher and the quality requirements imposed on the paper become ever stricter.
The present invention is direr;ted towards the further development of the evaporation drying and the dryer sections in paper machines so that the drying process in different parts of the drying section, in different phases of the drying process, and the dryer S section configuration can be optimized and the length of the dryer section shortened of kept unchanged while the speed become higher.
The invention additionally is .directed towards optimizing the runnability of the paper machine in different phases of the drying procedure so that the efficiency of the paper machine is improved while breaks are fewer and towards taking advantage of the different structures/methods/processes in the different phases of the paper drying process so that the quality properties of the paper can be optimized.
The nature of the drying procedures has been clarified further in the applicant's recent research and in dryer section that are in operation and in test runs on a test device. The invention is partly based on thc: observation that in the dryer section of a paper machine the drying process can be divided into three process stages that are different from each other:
(I) heating stage, in which evaporation does not take place to a substantial extent, but the water present in the web is mainly heated, (II) main evaporation area, in which the rate of evaporation remains substantially invariable when cylinder drying alone is used and in which the main evaporation of water from between the fibres and from their surface takes place, and (III) final evaporation area, in which the rate of evaporation becomes lower and the proportion of the evaporation that takes place on the drying cylinder is increased, and in this stage mainly evaporation of water present inside the fibres takes place.
It has also been a problem in the prior-art mufti-cylinder dryers that in said first stage (I) it has not been possible to use a temperature high enough in view of optimizing the drying, because, when the paper web is in direct contact with the hot faces on the drying cylinders, at temperatures higher than a certain figure, sticking of the web to the hot surface of the cylinder occurs, from which web breaks and standstill follow. It has been noticed that excessively hat contact drying cylinders also have detrimental effects on the quality properties of the paper.
The present invention is further directed towards the further development of said prior art, elimination of drawbacks of the prior art that were mentioned above and of those that will come out later, and implementation of other objectives of the invention.
In accordance with one aspect of the present invention, there is provided a method for evaporation drying a paper web having a dry solids content from about 35% to about 55% until the web has a dry solids content from about 90% to about 98%
comprising the steps of passing the web through three successive stages in a running direction of the web as follows:
in the first stage, passing the web through a short section in the machine direction and rapidly heating the web in the short section to a temperature from about 55° C. to about 85° C., in the second stage, drying the web utilizing an evaporation efficiency and rate of increase in dry solids content per unit of length of the dryer section in the machine direction which are higher than in the first stage or in the third stage and such that the temperature of the web does not rise substantially in the second stage, and in the third stage, continuing dying of the web with a decreasing evaporation efficiency and an average rate of increase in the dry solids content of the web in the machine direction which is lower than the rate of increase in the dry solids content of the web in the second stage.
The method aspect of the invention, therefore, is mainly characterized in that the method consists of three successive stages I, II and III, that are carried out in the direction of progress of the web in the sequence given as follows:
I in the first stage, the paper web coming from the press section of the paper machine is heated in a short section of the paper machine in the machine direction quickly to a temperature of 55° to 85° C, preferably to a temperature of about 70° C, and in this section the web i:c passed so that web breaks of the relatively moist and, thus, weak web are minimized, II after the first stage I, in this second stage II the main evaporation drying of the web is earned out with such m evaporation efficiency and rate of increase in dry solids content per unit of length o:f the dryer section in the machine direction that said evaporation efficiency and rate of increase in dry solids content of the web are substantially higher than in the first stage or in the final stage III, and the web temperature does substantially not rise in the second stage while the drying proceeds, III in the third and final stage, the drying is continued with a decreasing evaporation efficiency and with such an average rate of increase in the dry solids content of the web in the machine direction as is lower than in the preceding stage II
but higher than in a conventional cylinder drying with single-wire draw so that the paper quality can be controlled at the same time.
In accordance with another aspect of the present invention, there is provided a dryer section of a paper machine, comprising a first drying wire unit arranged to receive a web from a press section preceding the dryer section, said first drying unit comprising at least one of blow boxes and radiation dryer units for heating the web in a first stage without contacting the web, the web being passed in said first drying unit through a short section in the machine direction and rapidly heated in the short section to a temperature from about SS° C.. to about 85 ° C., and additional dryer units arranged after said first drying unit in the running direction of the web, said additional dryer units comprising at least one group with single-wire draw including contact drying cylinders arranged in a first row and reversing suction cylinders arranged in a second row below said first row of contact drying cylinders, a first set of said additional drier units being arranged to evaporation dry the web in a second stage utilizing an evaporation efficiency and rate of increase in dry solids content per unit of length of the dryer section in the machine direction which are higher than in the first stage and such that the temperature of the web does not rise substantially in the second stage, and g a second set of said additional dryer units arranged after said first set of additional dryer units and being arranged to continue drying the web in a third stage with a decreasing evaporation efficiency and an average rate of increasing in the dry solids content of the web in the machine direction which is lower than the rate of increase in the dry solids content of the web in the second stage.
A dryer section in accordance; with the aspect of the invention is mainly characterized in that, after the press section of the paper machine, the dryer section comprises the following dryer units that are placed in the given sequence in the machine direction:
in order to carry out the first si:age I of the method, the first unit is a drying wire unit in which the paper web runs past blow boxes and/or radiation dryer units, by whose means the web is heated without a direct contact with heated faces, in order to carry out the second stage II of the method, dryer units that comprise at least one single-wire group with single-wire draw that is open towards the bottom, in which the contact drying cylinders are in the upper row and the reversing suction cylinders are in the lower row so that removal of broke can take place downwards by the effect of gravity.
In the first stage I in the method in accordance with the invention, such a construction of the dryer section is used as also has optimal runnability properties so that in this stage, when the web is still moist and relatively weak, web breaks can be minimized.
The final stage III of the method of the invention is earned out with such solutions of equipment as also permit control of quality properties of paper, such as brightness, curl, etc.
With the method in accordance with the present invention and with a dryer section concept that carnes out the method it is possible to achieve the objectives mentioned above and to eliminate said drawbacks substantially. In accordance with the invention it is possible to provide a dryer section that is shorter and more compact than in the prior art also at high machine speeds so that the operating quality of the dryer section still remains good.
In the method and the dryer section in accordance with the invention the web is preferably dried so that in the first stage I the drying energy is at least mainly applied from the side of and through the upper surface of the web, in the second stage II the drying energy is applied to the; web from the side of and through its lower surface, and in the third stage III the drying energy is applied to the web from and through its both surfaces.
In the following, the invention will be described in detail with reference to some exemplifying embodiments of the invention illustrated in the figures in the accompanying drawings, the invention being by no means strictly confined to the details of said embodiments, wherein:
Figure lA is a schematic side view of a dryer section in accordance with the invention in which the method in accordance with the invention can be applied favourably;
Figure 1 B shows a preferred ~contact-drying/impingement-drying unit used in a dryer section in accordance with the invention, of which units there are three in the dryer section shown in Fig. 1, separated from one another by single-wire groups;
Figure 1 C shows the last wire group of the dryer section in a scale larger than Fig. 1 A, in which group the stage III of the method in accordance with the invention is earned out;
Figure 2 is a graphic illustration of the different stages of the method in accordance with the invention in a system of coordinates of dry solids content of the web - length of the dryer section in the machine direction, compared with a prior-art multicylinder dryer;
Figure 3 is a graphic illustration similar to Fig. 2 of the dryer method in accordance with the invention and of prior-art drying method in a system of coordinates o evaporation capacity - length of the dryer section in the machine direction;
Figure 4 is an illustration similar to Figs. 2 and 3 of the distribution of paper web temperature in the machine direction of the dryer section; and Figure 5 illustrates the evaporation capacity of stage III in accordance with the invention as a function of the: dry solids content percentage of the web in the method in accordance with the invention and in prior-art dryer section.
In the drawings, Figure lA shows a particularly favourable overall concept of a dryer section in accordance with the invention. As is shown in Fig. lA, the paper web W is passed from the press section 10 of the paper machine at a dry solids content of lco 35...55 % and at a temperature of To ~ 30...60°C on the bottom face of the transfer fabric 11 and supported by a PressRunTM box l la onto the top face of the drying wire 12 over its guide roll 13. The first planar drying unit R~ comprises a blow hood 15, under which the web W to be dried runs on the horizontal run of the wire 12, which is supported by the rolls 14. Said horizontal run of the wire 12 forms a plane consisting of grooved rolls and/or of suction boxes or blow boxes to support the web W.
In the unit Rl, an intensive drying energy impulse is applied to the web W in which connection, after the unit Rl, the temperature of the web W is Tl ~
60...85°C. In the unit Rl, primarily heating of the web W and of the water con-tained in it takes place, but no substantial evaporation of water as yet. The length L1 of the unit R1 in the machine direction is typically of an order of L1 .=
3...10 m.
In the unit R1, the paper web runs on support of the upper run of the drying wire 12 5 along a linear path in the horizontal plane so that it has no major changes in the direction and that, thus, no high dynamic forces are applied to it which might produce a web break in the web, which is still relatively moist and, thus, of low strength. In the interior of the blow hood 15, there is a nozzle arrangement, by whose means hot drying gases, such as air or steam, are blown against the top face 10 of the web. Additionally or alternatively, it is possible to employ infrared heaters.
Said blow devices and/or radiators in the unit Ri can be arranged so that their output in the cross direction of the web W is adjustable so as to provide profiling of the web W in the cross direction.
In Fig. lA, the unit R1 is followed by the first so-called normal (not inverted) single-wire unit R2, onto whose drying wire 22 the web W is transferred as a closed draw in the area of the first reversing suction roll 21. The single-wire unit R2, and so also the subsequent single-wire units R4, R6 and Rg that are open towards the bottom comprise steam-heated contact-drying cylinders 20 fitted in the upper row and reversing suction rolls 21 fitted in the lower row, for example the applicant's said YAC-rolls'. Below the cylinders 20, there are doctors and ventilation blow devices 25. The paper web W to be dried enters into direct contact with the faces of the steam-heated drying cylinders 20, and on the reversing suction rolls 21 the web W remains on the drying wire 22 at the side of the outside curve.
In Fig. lA, after the group R2 with single-wire draw, there follows a drying unit R3 in accordance with the invention, which, in accordance with Fig. 1B, comprises two contact-drying cylinders 30 and a large-diameter D1 impingement-drying/through-drying cylinder 31 with a perforated mantle, which cylinder will be called a large cylinder in the following. Around the contact-drying cylinders 30 and around the large cylinder 31, a drying wire 32 is fitted to run, which wire is guided by the guide rolls 33. The impingement-drying/through-drying hood module M1 of the _ T _ __. _~ _. __ _ _... ~ _ drying unit R3 is fitted in the basement space KT underneath the floor level of the paper machine hall on support of the floor level K2-K2 of said space.
The central axes of the contact-drying cylinders 30 in the unit R3 and in the correspon-ding following drying units RS and R7 in accordance with the present invention are placed substantially in the floor plane of the paper machine hall or in the vicinity of said plane K1-K1, preferably slightly above said plane. The paper web W to be dried is passed from the single-wire unit R2 as a closed draw onto the first drying cylinder 30 in the drying unit R3 (Rn), after which the web W is passed on the wire 32 of the unit R3 over the large cylinder 31 of the first module Ml on a remarkably large sector b .= 220...280° on support of the drying wire 32 and further onto the second drying cylinder 30 in the unit R3 (Rn). From this drying cylinder 30 the web W is transferred as a closed draw into the next normal unit R4 with single-wire draw, which unit is substantially similar to the unit R2 described above.
After this, there follows the second drying unit RS (Rn), which unit is similar to the drying unit R3 described above and whose large cylinder 31 is also placed in the basement space KT. After the drying unit Rg the web W is passed as a closed draw into the next single-wire unit R6, which is followed by the third drying unit R7 (Rn), whose large cylinder 31 is likewise placed in the basement space KT. The unit R7 is followed by a particular single-wire unit Rg, from which the web W°uc is passed to the reel-up or into a finishing unit (not shown). The construction and operation of the particular unit Rg will be described in more detail later with reference to Fig. 1C.
In the basement space, besides the modules M1, M2 and M3, Fig. lA also shows the pulpers 40a and 40b, between which there is the broke conveyor 41, which carries the paper broke into the pulper 40a and/or 40b. In the event of a web break, the web W can be passed after the unit R1 directly into the pulper 40a placed underneath.
The single-wire units R4, It6, and Rg are open towards the bottom, and therefore the paper broke falls from them by the effect of gravity onto the broke conveyor placed underneath or directly into the pulpers 40a,40b. Also the modules M1, and M3 are open or operable towards the bottom so that the paper broke falls out of connection with them, substantially by the effect of gravity, without major manual operations, onto the broke conveyor 41 placed underneath.
Underneath the modules M i , M2 and M3, above the floor level K2-K2 of the basement space KT, there is still space KTo for various devices, such as ducts through which the heating medium, such as heated air or steam, is passed into the interior of the hoods 35 of the modules M 1, M2 and M3 . Said lower space KT~
is defined from below by the floor level K2-K2 of the basement space and from above by the partition wall 42 placed below the broke conveyor 41. On the drying units R2...Rg there is an air-conditioned hood 50 in itself known.
Figure 1B is a more detailed illustration of the impingement-drying/through-drying hood module M in accordance with the invention. As is shown in Fig. IB, the wire 32a which runs around the large cylinder 31 is first passed around the last lower cylinder 21a in the preceding group Rn_1 with single-wire draw onto the first contact-drying cylinder 30 in the unit Rn, from it further as a short straight run over the sector b = 220 . . . 280 ° of the large cylinder 31 onto the second contact-drying cylinder 30 in the group Rn and over said cylinder on a sector of about 90°. After this the web W follows the face of the cylinder 10 and is transferred as a closed draw onto the drying wire 22 of the next group Rn+ 1. The hood of the large cylinder 3i, which consists of two parts 35, covers the cylinder substantially over the entire curve sector b of the wire 32a and the web W. On the sector b the web W
remains on the wire 32a at the side of the outside curve, so that its outer face is free. The large cylinder 31 is mounted on its axle journals 36, through which a communication is arranged with vacuum devices (not shown), by whose intermediate a suitable vacuum is produced in the interior of the cylinder 31, which vacuum is of an order of p~ ~ 1. ..3 kPa. This vacuum p~ keeps the web W on the wire 32a when the web W is at the side of the outside curve, and, at the same time, the vacuum p0 also promotes possible through-drying taking place through the web W and the wire 32a. The sector 360°-b that remains outside the sector b on the large cylinder 31 is covered by a cover plate 34 placed in the gap between the drying cylinders 30, and so also the last cylinder 21a in the group Rn, which can also be called the reversing cylinder of the group Rn, is covered by an obstacle plate 29. As to its more detailed embodiment, the perforated and grooved outer mantle 31a of the large cylinder is, for example, similar to that described in said FI Pat. Appl. 931263 and illustrated r _....____~ _____. _ _.__-~ 1 above all in Fig. 11 of said patent application, so that the construction will not be described again in this connection.
In accordance with figure 1B, the large cylinder 31 is mounted by means of its axle journals 36 on support of the frame construction 37. In this frame construction, both at the driving side and at the tending side, there are horizontal and machine direction beams 37a, on whose top face, or on rails provided on said top face, the hood halves 35 are arranged to be movable on wheels 39, which hood halves are illustrated in the open position 35a, in which the module M can be serviced. The hood halves 35 are displaced into the open and closed positions by actuating cylinders 38. The module M and its hood 35 are open towards the bottom, so that broke can be removed in the direction of the arrows WA substantially by the effect of gravity onto the broke conveyor 41 placed underneath without substantial manual operations. The top face of the hood 35 has been shaped as smoothly downwards inclined so as to improve the removal of broke.
Further, in the open position 35a of the hood 35, the module M can also be serviced and cleaned easily in other respects. The diameter D1 of the large cylinder 31 is, as a rule, chosen in the range of D 1 > 2 m, as a rule in the range of D 1 .= 2.
. . 8 m, preferably D1 = 2...4 m. The diameter D2 of the drying cylinders 30 in the group Rn is, as a rule, chosen in the range of D2 ~ 1.5...2.5 m, preferably in the range of D2 = 1.8...2.2 m. In the groups Rn_~ and Rn+1 with single-wire draw, the diameter of the drying cylinders 20 is preferably = D2. The diameter D3 of the reversing suction cylinders 21,21a is, as a rule, chosen in the range of D3 =
0.6...1.8 m, preferably D3 = 1Ø..1.5 m. The top face of the hood 35 has been shaped as smoothly downwards inclined to improve the removal of broke.
The wire 32a guide roll 33a placed above the latter drying cylinder 30 can be stationary or displaceable. Between the groups Rn_1, Rn and Rn+1 a little difference in speed can be employed, which is, typically, about 0.1..Ø2 %, so that, on the wires 22,32a,22, the speed becomes higher when the web W moves forwards. In the final end of the dryer section, the difference in speed can also be reversed.
The more detailed construction of the hood 35 of the module M and the circulation arrangements of the drying gases that are blown through it are described in detail in the FI Patent Application No. (971713) to be filed on the same day with the present application by the applicant, especially in its Fig. 3 and the related specification part, to which reference is made in this connection.
Fig. 1C shows, in a larger scale than Fig. lA, the last group Rg with single-wire draw in the dryer section in accordance with the invention, in which group the third stage of the invention is carried out. The paper web W to be dried is brought into the group R8 from the last contact-drying cylinder 30 of the module M3 shown in Fig. lA as a closed draw onto the first reversing suction roll 61 of the group Rg.
There are five of these reversing suction cylinders inside the wire loop 62 in the group Rg. The group Rg includes five contact drying cylinders 60,60A. Two middle ones 60A of these cylinders are contact drying cylinders whose diameter, which is larger than that of the other cylinders 60, is D4 .= 1.8...2.5 m, whereas the diam-eter of the smaller cylinders 60 is DS = 1Ø..1.8 m, and the diameter of the reversing suction cylinders 61 is D6 = 1Ø..1.5 m. Between the reversing suction cylinders 61 there are blowing devices 65 to ventilate the spaces between the cylinders 60,60A and 61 and to promote the drying. There is a blow box 64 above the upper sectors of the reversing suction cylinders 61 free from the web W
and from the wire 62, which promotes maintenance of the vacuum inside cylinders 61.
In order that it should be possible to carry out the stage III of the method in accord-ance with the invention and to achieve a sufficiently high evaporation capacity and an increase in the web W temperature Tw in accordance with the curve TI of Fig. 4 by means of the group Rg shown in Fig. 1C, a drying effect is applied to the web W
by means of contact drying cylinders 60A with large diameter also from the top face of the web W, i.e. from the drying wire 62. For this purpose ventilation hoods are provided above the cylinders 60A, into which hoods sufficiently hot and dry drying air gases are passed through the intake pipe 67. Out of the pressurized interior of the ventilation hoods 66, the humidified ventilation air is discharged into the hood 50 around the dryer section, from where it is removed in a way known T ___.___~~~__ _____.. . ._. _._...__ .___._~_ ~.._ .
from the prior art. These drying gases are blown against the drying wire 62 in the sector d of the cylinders 60A, said sector being preferably d = 180° or even larger.
Thus, evaporation of water is promoted through the upper face of the web W
through the wire 62. The ventilation hoods 66 are shown in their open position 66a, 5 as well as their air intake pipes are shown in their open position 67a. In this position 66a it is possible to clean and service the ventilation hoods, and the web W
thread-ing is also carried out most favourably then. In respect of their construction the ventilation hoods 66 can be similar to those that are described in more detail in the FI Patent Application (971713) to be filed on the same day with the present applica-10 lion.
In respect of the various details of the construction and the Qperation of the ventila-lion hoods 66, reference is made to the prior art coming out from the applicant's FI
Patent Application 951746 and from the FI Patent 83, 679 of Teollisuusmittaus Oy.
Fig. 2 shows the development of the dry solids content KA of the paper over the length L of the dryer section in the machine direction as a function. The curve K
represents an optimized method in accordance with the invention, and the curve KpA
represents the development of the dry solids content with a method and a dryer section of prior art. The curves K and Kpp have been obtained by means of com-puter simulation using the applicant's dryer section process model. The basis for the curve KpA is the applicant's prior-art SymRunT" dryer section concept, which consists of N pcs. of successive groups with single-wire draw that are open towards the bottom, and the curve K is based on a dryer section concept in accordance with Fig. 1.
It can be noticed immediately from Fig. 2 that it has been possible to shorten the length of the dryer section from the length LpA to the length LI, i.e. in practice by about 15...40 percent. In accordance with Figs. 1...4 the method in accordance with the invention is divided into three different stages I, II and III. As is seen in Fig. 2, in the first stage I the rate of increase in dry solids content KA of the web W
becomes higher from the initial value Kp more steeply in accordance with the curve K, in comparison with the curve KpA, because the initial temperature of the web W
is higher, which becomes clear from a comparison of the temperature curves TI
and TpA of the stage I in the figure. Also, in the first stage I, as is shown in Fig. 3, the evaporation efficiency PE is, in accordance with the curve PEI, substantially higher than in the prior-art method, curve PEpA of stage I (Fig. 3). In the invention the first phase I is carried out on a horizontal dryer unit R1 where the web W tem-perature Tw is raised to about 55...85°C, preferably to about 70°C, as comes out from Fig. 4. In the invention this raising of the temperature can be carried out very quickly, because in the unit RI a highly energy-intensive impingement stage and/or infra radiation can be used, because heating of the web W takes place free of contact so that there is no risk of sticking.
Stage II, shown in Figs. 1...4, is the main evaporation area where, in accordance with Fig. 2, the dry solids content KA of the web increases more steeply than in stage I as the drying proceeds. Fig. 3 shows the three successive evaporation peaks PEI, PF.z and PE3 of stage II, at which the maximal evaporation efficiency PE
is of an order of PE ~ 60 kg/m2/h (kilograms per square meter in an hour). These evaporation peaks are achieved by the hood modules M1, M2 and M3 in the dryer section shown in Fig. 1. Depending on the mode of operation of the modules M1, M2 and M3 or equivalent, the maximal evaporation efficiency can be even higher.
Between said peaks PE1, PE2 and PE3, the evaporation efficiency PE is of an order 20 kg/m2/h, i.e. of the same order of magnitude as the evaporation efficiency in accordance with the curve PEpA in Fig. 3 on the average.
In the exemplifying embodyment of Fig. 4, the web temperature TW stays substan-tially invariable in the stage II in accordance with the curves TI and TpA in a range of about 60...70°C. As was stated, the stage II is the main evaporation area where the water is evaporated from between the fibres in the web W and from the fibre surfaces.
In the third stage III in accordance with the invention, the steepness of the increase in the dry solids content decreases in comparison with stage II. The evaporation effi-_ T. ~
__.. . . ._ _ _. . _~ _ _ ciency also decreases in accordance with Fig. 3, whereas the web W temperature TW starts rising from about 70°C to 100...110°C. In the corresponding location in the dryer section in the machine direction, in prior-art methods, the evaporation effi-ciency still remains invariable, in accordance with the curve PEpp in Fig. 3, and so S also the temperature in accordance with the curve TpA in Fig. 4. In the dryer section in accordance with the invention, the stage III is carried out in the last cylinder group Rg, where the evaporation is made more intensive by means of the hoods that are placed above the cylinders 60 A with large diameter, in which hoods suffi-ciently powerful and hot drying gases are applied to the web W placed under the drying wire 62 and to the environment of the wire 62, so that the web W
tempera-ture TW can be raised very steeply in the stage III, in accordance with Fig.
4, in which connection also the water present inside the fibres in the paper web W
can be efficiently evaporated on a sufficiently short length L of the dryer section in the machine direction. Fig. 5 illustrates the evaporation efficiency PE in the stage III of the invention, i.e. the dry solids content KA in the area KA 80...98 %. The curve PRI represents the method in accordance with the invention, and the curve PEpA
a corresponding curve carried out by means of the prior-art SymRun'~ concept.
Fig. 5 shows that in the beginning of the stage III, in accordance with the curve PEI, in the dry solids content area 80.. .82 the evaporation efficiency is substantially higher than in the prior-art concept and somewhat higher than in the dry solids content area 84...91 and in the dry solids content area 93...98. This improvement has mainly been carried out in the particular group Rg by means of the drying cylinders with large diameter and by means of the blowings from their ventilation hoods 66.
Thus, in the drying method and in the dryer section in accordance with the inven-tion, the ultimate dry solids content of the web W, kl = 96...98 % , is achieved in the machine direction length LI of the dryer section, whereas in the prior art a substantially longer length LpA was needed.
As comes out from the above and especially from Fig. lA, the method stage I in accordance with the invention is carried out by applying drying energy mainly through the upper face of the web W. As is shown in Fig. 1, in the second stage II
of the method, drying energy is applied to the web mainly through the lower face of the web only by means of the wire groups Rg, R4, R5, R6, R~ and Rg and by means of the hood modules M1, M2 and M3, whereas in the group Rg (Fig. 1C) and in the stage III drying energy is applied to the web W through its both faces by applying drying energy through the lower face of the web W by means of the contact drying cylinders 60 and 60A and through the upper face of the web by means of the ventilation hoods 66 on the sectors d of the cylinders. This arrangement provides a short dryer section in which, at the same time, it is possible to control the paper quality, for example its curl.
In this context it should be emphasized that the method in accordance with the invention can also be carried out with many other dryer section concepts and solutions of equipment besides those of Figs. lA and 1B. Examples of these other dryer section concepts are some dryer section concepts described in the applicant's FI Patent Applications Nos. (971713 and 971715) to be filed on the same day with the present application. It is an essential feature of the dryer section in accordance with the invention that in said different drying stages I, II and III exactly a sort of a solution of equipment is used in which it is possible to carry out heating of the web and evaporation in accordance with the invention optimally. This inevitably has the consequence that, unlike the prior-art, in the different stages I, II and III of the invention, solutions of equipment different from one another have to be used, which is illustrated in Fig. 1.
In the following, the patent claims will be given, and the various details of the invention can show variation within the scope of the inventive idea defined in said claims and differ from the details described above by way of example only.
T.. T
__-_- ,~__.~.~____ ____ ..__..._ _.._
Claims (20)
1. A method for evaporation drying a paper web having a dry solids content from 35% to 55% until the web has a dry solids content from 90% to 98%, comprising the steps of:
passing the web through three successive stages in a running direction of the web as follows:
in the first stage, passing the web through a short section in the machine direction and rapidly heating the web in the short section to a temperature from about 55°C to about 85°C, in the second stage, drying the web utilizing an evaporation efficiency and rate of increase in dry solids content per unit of length of the dryer section in the machine direction which are higher than in the first stage or in the third stage and such that the temperature of the web does not rise substantially in the second stage, and in the third stage, continuing drying of the web with a decreasing evaporation efficiency and an average rate of increase in the dry solids content of the web in the machine direction which is lower than the rate of increase in the dry solids content of the web in the second stage.
passing the web through three successive stages in a running direction of the web as follows:
in the first stage, passing the web through a short section in the machine direction and rapidly heating the web in the short section to a temperature from about 55°C to about 85°C, in the second stage, drying the web utilizing an evaporation efficiency and rate of increase in dry solids content per unit of length of the dryer section in the machine direction which are higher than in the first stage or in the third stage and such that the temperature of the web does not rise substantially in the second stage, and in the third stage, continuing drying of the web with a decreasing evaporation efficiency and an average rate of increase in the dry solids content of the web in the machine direction which is lower than the rate of increase in the dry solids content of the web in the second stage.
2. The method of claim 1, wherein the step of heating the web in the first stage comprises the step of applying an energy-intensive heating effect of at least one of a drying gas and electromagnetic radiation to the web without contacting the web.
3. The method of claim 1 or 2, wherein the step of evaporation drying the web in the second stage comprises the step of applying evaporation efficiency peaks to the web to improve the evaporation of water from between fibers in the web and from fiber surfaces, the evaporation efficiency peaks being substantially higher than the evaporation efficiency applied to the web in the second stage between the evaporation efficiency peaks.
4. The method of any one of claims 1 to 3, wherein the step of drying the web in the third stage comprises the steps of contact drying the web by passing the web on a drying wire into direct contact with heated drying cylinders and applying drying gas flows to the web through the drying wire during the contact drying of the web.
5. The method of any one of claims 1 to 4, wherein the step of evaporation drying the web in the second stage comprises the step of applying evaporation power peaks to the web having a maximum evaporation efficiency from 50 to 90 kg/m2/h.
6. The method of any one of claims 1 to 5, wherein the step of evaporation drying the web in the second stage comprises the step of evaporation drying the web until the dry solids content is increased from 50% to 80%.
7. The method of any one of claims 1 to 6, wherein the step of evaporation drying the web in the second stage comprises the step of applying at least one evaporation efficiency peak to the web, each of the at least one evaporation efficiency peak being higher than the evaporation efficiency applied in the second stage between the evaporation efficiency peaks, each of the at least one evaporation efficiency peak being obtained by directing energy-intensive drying gas jets into contact with the web as the web runs through one of an impingement drying unit and a through-drying unit situated between a pair of contact drying cylinders and in a basement space below a floor level of the dryer section.
8. The method of any one of claims 1 to 7, wherein the step of drying the web in the third stage comprises the steps of:
passing the web into direct contact with heated contact drying cylinders, and regulating the evaporation rate by increasing a relative proportion of the contact of the web with the contact drying cylinders.
passing the web into direct contact with heated contact drying cylinders, and regulating the evaporation rate by increasing a relative proportion of the contact of the web with the contact drying cylinders.
9. The method of any one of claims 1 to 8, wherein the step of drying the web in the third stage comprises the steps of:
supporting the web on a drying wire, guiding the drying wire to press the web into direct contact with heated contact drying cylinders, and directing gas flows at the web through the drying wire as the drying wire carries the web over at least one of the contact drying cylinders.
supporting the web on a drying wire, guiding the drying wire to press the web into direct contact with heated contact drying cylinders, and directing gas flows at the web through the drying wire as the drying wire carries the web over at least one of the contact drying cylinders.
10. The method of any one of claims 1 to 9, wherein the step of drying the web in at least one of the second and third stages comprises the steps of:
passing the web through at least one single-wire draw group, and applying both impingement drying and through-drying of the web through a wire.
passing the web through at least one single-wire draw group, and applying both impingement drying and through-drying of the web through a wire.
11. The method of claim 1, wherein the step of heating the web in the first stage comprises the step of:
applying drying energy to the web mainly through its upper face;
the step of drying the web in the second stage comprises the step of:
applying drying energy to the web through its lower face; and the step of heating the web in the third stage comprises the step of:
applying drying energy to the web through both its upper and lower faces.
applying drying energy to the web mainly through its upper face;
the step of drying the web in the second stage comprises the step of:
applying drying energy to the web through its lower face; and the step of heating the web in the third stage comprises the step of:
applying drying energy to the web through both its upper and lower faces.
12. A dryer section of a paper machine, comprising:
a first drying wire unit arranged to receive a web from a press section preceding the dryer section, said first drying unit comprising at least one of blow boxes and radiation dryer units for heating the web in a first stage without contacting the web, the web being passed in said first drying unit through a short section in the machine direction and rapidly heated in the short section to a temperature from 55°C to 85°C, and additional dryer units arranged after said first drying unit in the running direction of the web, said additional dryer units comprising at least one group with single-wire draw including contact drying cylinders arranged in a first row and reversing suction cylinders arranged in a second row below said first row of contact drying cylinders, a first set of said additional dryer units being arranged to evaporation dry the web in a second stage utilizing an evaporation efficiency and rate of increase in dry solids content per unit of length of the dryer section in the machine direction which are higher than in the first stage and such that the temperature of the web does not rise substantially in the second stage, and a second set of said additional dryer units arranged after said first set of additional dryer units and being arranged to continue drying the web in a third stage with a decreasing evaporation efficiency and an average rate of increase in the dry solids content of the web in the machine direction which is lower than the rate of increase in the dry solids content of the web in the second stage.
a first drying wire unit arranged to receive a web from a press section preceding the dryer section, said first drying unit comprising at least one of blow boxes and radiation dryer units for heating the web in a first stage without contacting the web, the web being passed in said first drying unit through a short section in the machine direction and rapidly heated in the short section to a temperature from 55°C to 85°C, and additional dryer units arranged after said first drying unit in the running direction of the web, said additional dryer units comprising at least one group with single-wire draw including contact drying cylinders arranged in a first row and reversing suction cylinders arranged in a second row below said first row of contact drying cylinders, a first set of said additional dryer units being arranged to evaporation dry the web in a second stage utilizing an evaporation efficiency and rate of increase in dry solids content per unit of length of the dryer section in the machine direction which are higher than in the first stage and such that the temperature of the web does not rise substantially in the second stage, and a second set of said additional dryer units arranged after said first set of additional dryer units and being arranged to continue drying the web in a third stage with a decreasing evaporation efficiency and an average rate of increase in the dry solids content of the web in the machine direction which is lower than the rate of increase in the dry solids content of the web in the second stage.
13. The dryer section of claim 12, wherein said second set of additional dryer units comprises said at least one single-wire draw group, said at least one single-wire draw group including a hood arranged to increase evaporation through the wire and extending above at least one of said contact drying cylinders in said at least one single-wire draw group.
14. The dryer section of claim 12 or 13, wherein said second set of additional dryer units comprises said at least one single-wire draw group, said at least one single-wire draw group including a hood arranged to increase evaporation through the wire and extending above a first one of said contact drying cylinders in said at least one single-wire draw group, said first one of said contact drying cylinders having a diameter larger than a diameter of at least a second one of said contact drying cylinders in said at least one single-wire draw group.
15. The dryer section of any one of claims 12 to 14, wherein said additional dryer units comprise at least two of said single-wire draw groups, further comprising:
a drying module arranged between said single-wire draw groups, said drying module comprising:
a drying wire guided in a loop, a large-diameter cylinder arranged in said loop of said drying wire, said drying wire being guided over said large-diameter cylinder such that a contact sector of said drying wire over said large-diameter cylinder is greater than 180°, said large-diameter cylinder being selected from a group consisting of an impingement-drying cylinder and a through-drying cylinder, a blow hood arranged around said large-diameter cylinder and having an open position and a closed position, and a pair of heated contact-drying cylinders having a diameter smaller than a diameter of said large-diameter cylinder, each of said pair of contact-drying cylinders being situated on a respective side of said large-diameter cylinder at least one of above said large-diameter cylinder and proximate said large-diameter cylinder.
a drying module arranged between said single-wire draw groups, said drying module comprising:
a drying wire guided in a loop, a large-diameter cylinder arranged in said loop of said drying wire, said drying wire being guided over said large-diameter cylinder such that a contact sector of said drying wire over said large-diameter cylinder is greater than 180°, said large-diameter cylinder being selected from a group consisting of an impingement-drying cylinder and a through-drying cylinder, a blow hood arranged around said large-diameter cylinder and having an open position and a closed position, and a pair of heated contact-drying cylinders having a diameter smaller than a diameter of said large-diameter cylinder, each of said pair of contact-drying cylinders being situated on a respective side of said large-diameter cylinder at least one of above said large-diameter cylinder and proximate said large-diameter cylinder.
16. The dryer section of claim 15, wherein the paper machine is situated in a paper machine hall having a floor level, said large-diameter cylinder in said drying module being arranged below the floor level of the paper machine hall, said contact drying cylinders of said single-wire draw groups being arranged such that the central axes of said contact drying cylinders are situated above said large-diameter cylinder in said drying module and above the floor level of the paper machine hall.
17. The dryer section of claim 16, further comprising a broke conveyor arranged underneath said single-wire draw groups and said blow hood of said drying module such that while in the hood open position, the removal of broke from said blow hood takes place by the force of gravity onto said broke conveyor.
18. The dryer section of any one of claims 12 to 17, wherein said first set of additional dryer units comprises first, second and third single-wire draw groups and said second set of additional dryer units comprises at least one single-wire draw group, further comprising:
first, second and third drying modules each comprising:
a drying wire guided in a loop, a large-diameter cylinder arranged in said loop of said drying wire, said drying wire being guided over said large-diameter cylinder such that a contact sector of said drying wire over said large-diameter cylinder is greater than 180°, said large-diameter cylinder being selected from a group consisting of an impingement-drying cylinder and a through-drying cylinder, a blow hood arranged around said large-diameter cylinder and having an open position and a closed position, and a pair of heated contact-drying cylinders having a diameter smaller than a diameter of said large-diameter cylinder, each of said pair of contact-drying cylinders being situated on a respective side of said large-diameter cylinder at least one of above said large-diameter cylinder and proximate said large-diameter cylinder, said first drying module being arranged after said first single-wire draw group, said second single-wire draw group being arranged after said first drying module, said second drying module being arranged after said second single-wire draw group, said third single-wire draw group being arranged after said second drying module, said third drying module being arranged after said third single-wire draw group, said at least one single-wire draw group of said second set of additional dryer units being arranged after said third drying module, said at least one single-wire draw group including a hood arranged extending above a first one of said contact drying cylinders in said at least one single-wire draw group, said first one of said contact drying cylinders having a diameter larger than a diameter of at least a second one of said contact drying cylinders in said at least one single-wire draw group.
first, second and third drying modules each comprising:
a drying wire guided in a loop, a large-diameter cylinder arranged in said loop of said drying wire, said drying wire being guided over said large-diameter cylinder such that a contact sector of said drying wire over said large-diameter cylinder is greater than 180°, said large-diameter cylinder being selected from a group consisting of an impingement-drying cylinder and a through-drying cylinder, a blow hood arranged around said large-diameter cylinder and having an open position and a closed position, and a pair of heated contact-drying cylinders having a diameter smaller than a diameter of said large-diameter cylinder, each of said pair of contact-drying cylinders being situated on a respective side of said large-diameter cylinder at least one of above said large-diameter cylinder and proximate said large-diameter cylinder, said first drying module being arranged after said first single-wire draw group, said second single-wire draw group being arranged after said first drying module, said second drying module being arranged after said second single-wire draw group, said third single-wire draw group being arranged after said second drying module, said third drying module being arranged after said third single-wire draw group, said at least one single-wire draw group of said second set of additional dryer units being arranged after said third drying module, said at least one single-wire draw group including a hood arranged extending above a first one of said contact drying cylinders in said at least one single-wire draw group, said first one of said contact drying cylinders having a diameter larger than a diameter of at least a second one of said contact drying cylinders in said at least one single-wire draw group.
19. The dryer section of any one of claims 12 to 18, further comprising at least one hood for one of through-drying and impingement-drying arranged in connection with at least one of said contact drying cylinders in said at least one single-wire draw group.
20. The dryer section of any one of claims 12 to 19, further comprising:
at least one impingement-drying hood arranged in connection with at least one of said contact drying cylinders in said at least one single-wire draw group, and further comprising:
at least one through-drying hood arranged in connection with at least one of said contact drying cylinders in said at least one single-wire draw group.
at least one impingement-drying hood arranged in connection with at least one of said contact drying cylinders in said at least one single-wire draw group, and further comprising:
at least one through-drying hood arranged in connection with at least one of said contact drying cylinders in said at least one single-wire draw group.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| FI971714 | 1997-04-22 | ||
| FI971714A FI971714A (en) | 1997-04-22 | 1997-04-22 | Procedure for optimizing the paper evaporation drying, driveability and quality, and drying portion applying the procedure in a paper machine |
| PCT/FI1998/000351 WO1998048107A1 (en) | 1997-04-22 | 1998-04-21 | Method for optimizing evaporation drying of paper, runnability, and paper quality as well as dryer section that makes use of the method in a paper machine |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CA2287355A1 CA2287355A1 (en) | 1998-10-29 |
| CA2287355C true CA2287355C (en) | 2007-03-13 |
Family
ID=8548699
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA002287355A Expired - Fee Related CA2287355C (en) | 1997-04-22 | 1998-04-21 | Method for optimizing evaporation drying of paper, runnability, and paper quality as well as dryer section that makes use of the method in a paper machine |
Country Status (8)
| Country | Link |
|---|---|
| EP (1) | EP1012386B1 (en) |
| JP (1) | JP3604704B2 (en) |
| AT (1) | ATE315123T1 (en) |
| AU (1) | AU7045998A (en) |
| CA (1) | CA2287355C (en) |
| DE (1) | DE69833107T2 (en) |
| FI (1) | FI971714A (en) |
| WO (1) | WO1998048107A1 (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FI105217B (en) | 1998-12-04 | 2000-06-30 | Valmet Corp | A method for controlling the drying process of a papermaking machine or the like in a drying section |
| FI111970B (en) * | 1998-12-04 | 2003-10-15 | Metso Paper Inc | A method and apparatus for controlling the drying process of a papermaking machine or the like in a drying section |
| FI124218B (en) | 2007-01-22 | 2014-05-15 | Valmet Technologies Inc | System in a drying section of a web forming machine for controlling the wire and further web by directional rollers |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE3721734A1 (en) * | 1987-07-01 | 1989-01-12 | Voith Gmbh J M | METHOD FOR DRYING A RUNNING TRAIN AND PAPER OR CARDBOARD MACHINE FOR CARRYING OUT THE METHOD |
| WO1989004890A1 (en) * | 1987-11-26 | 1989-06-01 | Valmet Oy | Method and device in on-machine coating-drying of a paper web or equivalent |
| FI102623B (en) * | 1995-10-04 | 1999-01-15 | Valmet Corp | Method and apparatus in a paper machine |
-
1997
- 1997-04-22 FI FI971714A patent/FI971714A/en unknown
-
1998
- 1998-04-21 AT AT98917149T patent/ATE315123T1/en not_active IP Right Cessation
- 1998-04-21 CA CA002287355A patent/CA2287355C/en not_active Expired - Fee Related
- 1998-04-21 JP JP54509598A patent/JP3604704B2/en not_active Expired - Fee Related
- 1998-04-21 WO PCT/FI1998/000351 patent/WO1998048107A1/en active IP Right Grant
- 1998-04-21 EP EP98917149A patent/EP1012386B1/en not_active Expired - Lifetime
- 1998-04-21 DE DE69833107T patent/DE69833107T2/en not_active Expired - Lifetime
- 1998-04-21 AU AU70459/98A patent/AU7045998A/en not_active Abandoned
Also Published As
| Publication number | Publication date |
|---|---|
| CA2287355A1 (en) | 1998-10-29 |
| FI971714A0 (en) | 1997-04-22 |
| DE69833107T2 (en) | 2006-08-17 |
| DE69833107D1 (en) | 2006-03-30 |
| WO1998048107A1 (en) | 1998-10-29 |
| EP1012386B1 (en) | 2006-01-04 |
| JP3604704B2 (en) | 2004-12-22 |
| ATE315123T1 (en) | 2006-02-15 |
| AU7045998A (en) | 1998-11-13 |
| FI971714A (en) | 1998-10-23 |
| EP1012386A1 (en) | 2000-06-28 |
| JP2001504175A (en) | 2001-03-27 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| EEER | Examination request | ||
| MKLA | Lapsed |