Title of Invention

A METHOD FOR SUPPLYING A PULP SUSPENSION TO A HEADBOX OF A PAPERMAKING OR BOARD MACHINE AND A DEGASSING DEVICE

Abstract The method serves for supplying a pulp suspension (S) to a headbox (1) of a papermaking or board machine (2) or to a filter device. The pulp suspension (S) can be formed e.g. by mixing a slush pulp suspension (4) with a diluting liquid (5). The method uses at least one degassing device (6), the effect of which corresponds to that of a centrifuge. The method can be implemented in a space- saving manner and makes it possible e.g. to omit large degassing tanks.
Full Text RPS12086 EP
VOITH PATENT GmbH
Method for degassing and supplying a pulp suspension to a headbox or a filter
device, and also degassing device
The invention relates to a method for supplying a pulp suspension in accordance
with the preamble of Claim 1, 3 or 14, and also to a degassing device in
accordance with the preamble of Claim 26.
Such methods are used e.g. for supplying papermaking or board machines with
pulp suspension. The headbox conveys a layer of pulp onto a wire running past,
which inter alia also performs the function of thickening. The stock supply
systems required for this are known in principle. The pulp suspension to be
supplied receives the major portion of the fibres from a slush pulp suspension
provided in the stock preparation plant. The latter has e.g. a typical consistency
of between 2.5 and 5%. By admixing diluting liquid, e.g. white water from the
papermaking machine, the consistency is reduced to a value which is beneficial
for operation of the headbox of the papermaking machine. Although white water
is optimally suited for this dilution function, there are problems owing to the high
gas content, the predominant portion being air. The major part of these gases
escape very rapidly, but on the other hand the residual gases often have to be
removed in a costly manner. Otherwise, the quality of the paper produced would
be impermissibly reduced. Known solutions are large degassing tanks in which a
constant partial vacuum which corresponds to the vapour pressure of the
suspension to be degassed is maintained by evacuation. This is effective, but
expensive.
A degassing pump for producing paper is known from US 6,723,205 B1, which
pump is provided with a rotor forming a cylindrical interior in which the supplied

liquid can be degassed by centrifugal force. The white water supplied at high
speed from the papermaking machine provides the driving power for the rotor by
means of a turbine integrated in the degassing pump. After emerging from the
degassing pump, the liquid is passed directly into mixing stations in which the
fibrous raw material (slush pulp) is admixed.
Another application of methods of this type takes place in the preparation plant
("stock preparation") for the pulp suspension intended for processing on the
papermaking or board machine. For suspensions with a relatively low
consistency, e.g. between 0.5% and 1.5%, filter devices, particularly disc filters,
are used to increase consistency. In such case, the pulp suspension to be
thickened may have an air content of several percent, e.g. if it has undergone
flotation beforehand in order to separate out anionic trash with the flotation froth.
The operation of disc filters and pumps is adversely affected by a relatively high
air content.
It is an object of the invention to provide a method of the type referred to first
hereinbefore with which a stock stream which is sufficiently degassed is carried
to the headbox or to a filter device. It should be able to operate at relatively low
cost and be reliable.
A method having the features of the independent claims is provided in order to
achieve this object.
The stock supply system according to the invention is distinguished particularly in
that a degassing device which is of compact construction and yet permits good
degassing is used for degassing the white water or the pulp suspension. In
particular, it is generally not necessary to use large, expensive tanks which in
operation place a great load on the building owing to their great weight. Such
tanks are operated with the vapour pressure of the suspension to be degassed,
and are therefore placed under an extreme partial vacuum, with the resultant
strength requirements. Also vacuum systems with high energy consumption are
not required for the method according to the invention.

The method can be applied particularly beneficially to papermaking machines
having a wire speed of between 800 and 1600 m/min. The amount of air
contained in the white water depends greatly on the wire speed.
The method can also be applied if a pulp suspension - as is known per se - is
passed over a disc filter in order to thicken it. Such a disc filter permits a
significantly higher throughput if the air content of the incoming liquid is reduced.
One further essential advantage of the invention is that the stock pump
connected to the degassing device not only transports the deaerated fibre
suspension emerging from the degassing tank further, but that a lower pressure
which promotes degassing can be set in the degassing device, since the pump
exerts suction.
In one advantageous embodiment, the rotor of the degassing device is driven by
a motor, e.g. an electric motor. The peripheral speed of the rotor can thus be
adjusted simply to a value which meets requirements.
The invention will be explained with reference to drawings. These show:
Fig. 1 a simplified process diagram;
Fig. 2 a variant;
Fig. 3 a degassing device according to the invention;
Fig. 4 a degassing device according to the invention with screening
function;
Fig. 5 another embodiment of the method;
Fig. 6 an application of the method in stock preparation.

The diagram of Fig. 1 depicts a first example for performing the method
according to the invention. A pulp suspension S is produced in the usual manner
by mixing a slush pulp suspension 4 with a diluting liquid 5, and then has
substantially the consistency desired for operating the headbox 1 of the
papermaking or board machine 2 at this point. It is known that headbox
consistencies are in the range of between 0.5 and 2%, as a rule around 1%. The
diluting liquid 5, which is supplied at a mixing point 8, in the example illustrated
here originates from the first white water 12, i.e. the water produced in the
forming region of the papermaking or board machine 2. It is often referred to as
white water I (SW I), in contrast to the second white water 12' (SW II) produced
later on the papermaking machine, which contains far fewer fines.
It is known that such white water is mixed inter alia with a considerable
proportion of air and possibly other gases. The white water is collected beneath
the papermaking machine wire and discharged at the side. A large proportion of
the air contained therein can emerge already in the open channels used therefor.
Nevertheless, it is often useful to separate off a further portion of gas 7' in a
special tank 11, as is known e.g. from DE 199 38 799 . The tank 11 may be
under a moderate partial vacuum for support. Once the slush pulp suspension 4
and diluting liquid 5 have been mixed, a degassing device 6 is used. This is
constructed as a cylindrical or conical tank and is provided according to the
invention with a rotor 13. A motor 34, which is not supplied with power from the
hydraulic energy of the degassed suspension flow, e.g. an electric motor, serves
to drive the rotor 13. The pulp suspension S passes into the substantially
cylindrical interior 14 of the rotor 13 and is caused to rotate at high speed. This
principle corresponds to that of a solid-bowl centrifuge. The gases 7 contained
therein migrate inwards as a result of the centrifugal forces [sic] and are
extracted from the centre by a - only roughly indicated - vacuum means 10. In so
doing, a liquid/gaseous interface forms in the tank. The centrifugal forces may be
at least 5 times, preferably 10 times, as great as the acceleration due to gravity.
The vacuum means 10 does not require a partial vacuum which corresponds to
the vapour pressure of the suspension or is close thereto. Usual values for the

5
partial vacuum of a vacuum means 10 used here are 0.8 to 0.9 bar.
After leaving the degassing device 6, the suspension is carried via a stock pump
9 here in a closed system (i.e. without open tanks or chests) to the headbox 1. In
so doing, here in the usual manner the remainder of anionic trash which is still
present is separated off by a cleaner unit 17 and a screening plant 18. In order to
prevent the pressure in the cleaner unit 17 from becoming too high, a pump 22
("booster pump") may be installed between the accepted stock from the cleaner
unit 17 and the infeed to the screening plant 18 in order to increase the pressure.
Alternatively, an open intermediate chest 20 may also be provided after the stock
pump 9 for guiding the stock, e.g. in order to reduce pulsations. This is depicted
in Fig. 2, but can also be realised in an installation according to Fig. 1. Of course,
the cost which has to be incurred for these hydrocyclones and screens will
depend on the raw materials and the quality demands on the paper produced. If
e.g. the slush pulp suspension 4 has been formed from waste paper, sand and
small pieces of plastic may still be present.
The invention can also be carried out such that - as Fig. 2 shows - the white
water 12 from the papermaking or board machine 2 is degassed in a degassing
device 6', the function of which corresponds to that of the one already described
in conjunction with Fig. 1. The degassed white water is passed through the outlet
15 directly into a diluting-water pump 19. Owing to the far lower solids content of
the white water 12 compared with the pulp suspension S, the degassing can be
performed more easily. This however assumes an at most only low gas content
in the slush pulp suspension 4 which is added at the mixing point 8, in order to
avoid losses of quality.
It is known that there are many papermaking or board machines in which the
headbox is supplied not only with the pulp suspension S already mentioned, but
also additionally with a diluting liquid, which is metered in at different points
viewed across the width of the headbox 1. E.g. the transverse profile of the layer
of pulp formed with the headbox can be influenced, in particular optimised,
thereby. Such a possibility is shown in Fig. 2, in which the white water is used

not only as diluting liquid 5 for the slush pulp suspension 4. A portion of the white
water deaerated in the degassing device 6' is passed by the diluting-water pump
19 as diluting liquid 5' into a metering means 3 of the headbox 1', in which it is
split up and metered into the pulp suspension S at various points. Often there are
further points in a paper mill at which further diluting liquid 5" deaerated by the
method can be used, which is indicated here by a broken-line arrow.
Fig. 3 shows, without representing structural details, a degassing device 6
suitable for the method in section. A rotor 13 is located in a fixed housing 23, the
interior 14 of which rotor is supplied with a liquid which is to be degassed through
the inlet 16. The inlet 16 may be arranged centrally or, as here, eccentrically.
The liquid which is added therethrough is initially accelerated greatly in the
peripheral direction, which purpose may be served by e.g. accelerating ribs 24.
As a result of the centrifugal forces, the liquid is applied to the inner wall of the
rotor 13, the gas contained therein, in particular the air, migrating towards the
centre of the rotor 13. As a rule, an interface forms between the liquid and the
gas 7. The gas 7 can be removed or extracted through a central degassing pipe
25. In continuous operation of this degassing device, the operating conditions
can be regulated e.g. by an input choke 26 such that a constant stream of liquid
forms from the inlet 16 to the outlet 15. In that case, the wall of the rotor 13 is
made to be permeable to liquid in the region of the outlet 15, e.g. by forming
openings 27 in this region. The outlet 15 is advantageously tangentially attached,
such that the rotational flow of the degassed liquid leads to a pressure build-up in
the outlet 15. The openings 27 in the wall of the rotor 13 are so large that they do
not result in screening of the degassed liquid.
The embodiment of a degassing device 61 depicted in Fig. 4 combines the
function of degassing with the function of screening. As has already been
mentioned, when supplying a papermaking machine often a final screening stage
is inserted before the headbox, in order to prevent anionic trash which might
disrupt the operation of the headbox or the papermaking machine from entering
it. This screening function can be performed in combination with the degassing
function in the same device. For this, a screen basket 28 is arranged such that

the degassed liquid flowing radially outwards from the rotor 13' is supplied to the
screen basket 28. In known manner, separation into accepted stock 29 and
rejects 30 takes place at the screen openings 32 of the screen basket 28. The
latter can be discharged from the device through a rejects outlet 31. Only some
of the screen openings 32 in the screen basket 28 are depicted by way of
example, and not to scale. The combination has the advantage that the rotor 13'
can also serve to keep the screen openings 32 clear. For this, scraper elements
33 which are capable of generating suitable suction and pressure pulses in the
fibre suspension are attached to its outside.
Fig. 5 depicts a process diagram with the use of a degassing device 6'
constructed according to Fig. 4. Then the screens for the pulp suspension S
depicted in Fig. 1 can be omitted. Possibly, furthermore a cleaner unit 17 will be
necessary between the degassing device 6' and the headbox 1; however, this
depends on the anionic trash present in the pulp suspension S.
Fig. 6 depicts a beneficial application of the invention in the stock preparation
stage of a paper mill. A low-consistency pulp suspension S" is thickened, i.e.
brought to a higher consistency, in a disc filter 35 which is merely indicated. The
stock S"1 thickened by the filter action can be prepared further as a raw material
for paper production, while the filtrate 36 serves e.g. for dilution. The reason for
such a measure is that the method steps in the stock preparation stage optimally
take place in part at low and in part at higher consistency.
In the installation depicted in Fig. 6, a flotation plant 37 is operated which cleans
a pulp suspension S' mixed with anionic trash, e.g. ink particles, at low
consistency, e.g. between 0.5 and 2%. Five flotation cells 38 of the flotation plant
37 through which the flow passes in succession are illustrated diagrammatically.
In each case, the accepted stock from an upstream flotation cell is conveyed by
a plurality of pumps 39 by means of an aeration injector 40 into the next flotation
cell. The rejects R formed, i.e. the flotation froth, contains the anionic trash which
has been separated off. The accepted stock from the final flotation cell 38', which
has e.g. an air content of between 3% and 6%, is withdrawn here by a stock

8
pump 9 succeeding the degassing device 6. This reduces the pressure of the
degassing device 6, which further promotes the degassing effect.
The degassing device 6 inserted between the flotation plant 37 and disc filter 35
removes a large portion of the air taken up e.g. in the flotation plant 37. The disc
filter 35 already permits a 10% higher throughput e.g. for a reduction of the air
content by one percentage point. If e.g. a reduction from 6% to 1% takes place,
the possible throughput is approx. 50% higher. Also other problems associated
with the relatively high air content, e.g. at the stock pump 9, are overcome
effectively and economically. The degassing device 6 described is particularly
economical for just such tasks, in which the last percentage fraction of the air
content in the degassed liquid does not matter too much.
Often fine screening 41 is effected after the flotation and before the thickening,
this being particularly effective at low consistency (e.g. 0.5 to 2%).

9
Claims:
1. A method for supplying a pulp suspension to at least one headbox (1, 1')
of a papermaking or board machine (2) with at least one dilution means, in which
the pulp suspension (S) is produced by mixing a slush pulp suspension (4) with a
diluting liquid (5), in particular water, and at least one means for removing gas
from liquid,
characterised in that
the pulp suspension (S) after mixing with the diluting liquid (5) is passed into at
least one degassing device (6), in which it passes into the interior (14) of a
rotating rotor (13, 13') and is caused to rotate, so that the gases (7) contained
therein are separated off due to centrifugal forces and that the degassed diluting
liquid (5) is passed from the degassing device (6) into a separate stock pump (9).
2. A method according to Claim 1,
characterised in that
the pulp suspension (S) after the degassing device (6) is passed through a stock
pump (9) in a closed system to the headbox (1, 1') and that the degassing device
(6) is arranged, viewed in the direction of flow of the pulp suspension, directly
before the stock pump (9).
3. A method for supplying a pulp suspension (S) to at least one headbox (1,
1') of a papermaking or board machine (2) with at least one dilution means, in
which the pulp suspension (S) is produced by mixing a slush pulp suspension (4)
with a diluting liquid (5), in particular water, and at least one means for removing
gas from liquid,
the diluting liquid (5) before mixing with the slush pulp suspension (4) being
passed into at least one degassing device (6), in which it passes into the interior
(14) of a rotating rotor (13, 13') and is caused to rotate, so that the gases (7)
contained therein are separated off due to centrifugal forces,
characterised in that
the degassed diluting liquid (5) is passed out of the degassing device (6) into a
separate diluting-water pump (19).

10
4. A method according to Claim 3,
characterised in that
the headbox (1') is provided with a metering means (3) with which the headbox
(1') is supplied with diluting liquid (51) in order to regulate the transverse profile of
the web which is produced, for the provision of which the degassing device (61)
for the diluting liquid is used.
5. A method according to Claim 3 or 4,
characterised in that
further diluting liquid (5") is degassed in the degassing device (61) in order to
supply further dilution points.
6. A method according to one of the preceding claims,
characterised in that
a wet screening operation to remove anionic trash from the pulp suspension (S)
is performed in the degassing device (61), in that the degassed liquid is passed
from the interior (14') to a screen basket (28) incorporated in the degassing
device (61).
7. A method according to Claim 6,
characterised in that
the rotor (13') is also used to keep the screen basket (28) clear.
8. A method according to Claim 6 or 7,
characterised in that
the screen basket (28) is inserted radially outside the rotor (131).
9. A method according to one of the preceding claims,
characterised in that
the diluting liquid (5) is white water (12) from the papermaking or board machine
(2).

11
10. A method according to Claim 9,
characterised in that
the white water (12) is pre-degassed in open channels before entering the
degassing device (6') or the mixing point (8).
11. A method according to one of the preceding claims,
characterised in that
the pulp suspension (S) is carried to the headbox (1, 1') with the aid of a stock
pump (9) in a closed system, without being degassed by re-application of a
partial vacuum.
12. A method according to one of the preceding claims,
characterised in that
the pulp suspension (S) after the degassing device (6, 6') is passed through a
cleaner unit (17) with the aid of a directly following stock pump (9) and that the
accepted stock from this cleaner unit (17) is not degassed further by applying a
partial vacuum.
13. The application of the method in the operation of a papermaking machine,
the wire speed of which is between 800 and 1600 m/min.
14. A method for supplying a pulp suspension to at least one filter device,
preferably a disc filter (35),
the pulp suspension (S) being thickened by a filtration operation,
the pulp suspension having a consistency of at most 4%, preferably between 0,5
and 2%,
characterised in that
the pulp suspension (S) before thickening is passed into at least one degassing
device (6), in which it passes into the interior (14) of a rotating rotor (13, 13') and
is caused to rotate, so that the gases (7) contained therein are separated off due
to centrifugal forces.

12
15. A method according to Claim 14,
characterised in that
the degassed diluting liquid (5) is passed out of the degassing device (6) into a
separate stock pump (9).
16. A method according to Claim 14 or 15,
characterised in that
a pulp suspension (S'), particularly a waste paper suspension, is cleaned in a
flotation plant (37) of anionic trash removed with the flotation froth and is then
thickened.
17. A method according to Claim 16,
characterised in that
the pulp suspension (S) cleaned in the flotation plant (37) is passed into the
degassing device (6) without an interposed pump.
18. A method according to one of the preceding claims,
characterised in that
the pulp suspension (S) passed into the degassing device (6) has a gas content
of more than 1.5%.
19. A method according to Claim 18,
characterised in that
the pulp suspension (S) passed into the degassing device (6) has a gas content
of more than 3%, preferably more than 5%.
20. A method according to one of the preceding claims,
characterised in that
the absolute pressure in the degassing device (6, 6') is set to at least 0.1 bar
above the vapour pressure of the pulp suspension located therein.
21. A method according to one of the preceding claims,

13
characterised in that
a degassing device (6, 6') is used with a rotor (13) having a cylindrical interior
(14), the wall of which rotor is impermeable to liquid.
22. A method according to one of Claims 1 to 21,
characterised in that
a degassing device (6, 6') is used with a rotor (13) having a cylindrical interior
(14), the wall of which rotor is permeable to liquid only in the region of the outlet
(15) through which the degassed liquid is removed.
23. A method according to one of the preceding claims,
characterised in that
the rotor (13, 13') is driven by a motor (34).
24. A method according to one of the preceding claims,
characterised in that
the rotor (13, 13') is driven such that a centrifugal field of at least 50 times,
preferably at least 10 times, the acceleration due to gravity is produced in its
interior (14, 14").
25. A method according to one of the preceding claims,
characterised in that
the degassing device (6, 6') is operated continuously.
26. A degassing device for performing a method according to one of the
preceding claims,
with a housing (23) in which a rotor (13, 13') having an interior (14) is rotatably
arranged,
with an inlet (16) for adding a liquid to be degassed, the inlet (16) opening into
the interior (14) of the rotor (13, 13'),
and also with a preferably tangentially attached outlet (15) for the degassed
liquid,

14
and also with a centrally arranged degassing pipe (25), to which a vacuum
means (10) for removing the gas (7) which has escaped from the liquid is
connected, the rotor (13) being provided with at least one opening (27) through
which a hydraulic connection to the outlet (15) is produced,
characterised in that
the rotor (13) is connected to a motor (34) which drives it.
27. A degassing device according to Claim 26,
characterised in that
the rotor (13, 13') is surrounded by a screen basket (28), the screen openings
(32) of which produce a hydraulic connection between the rotor (13, 13") and
outlet (15) and which are suitable for screening a pulp suspension (S) such that
the major part of the fibres pass through the screen openings (32) and can be
removed as accepted stock (29), whereas the anionic trash is retained as rejects
(30) and can be discarded through a rejects outlet (31).
28. A degassing device according to Claim 27,
characterised in that
the openings (27) in the screen basket (28) are round holes with a diameter of
between 1 and 4 mm.
29. A degassing device according to Claim 27 or 28,
characterised in that
the rotor (131) is provided on its outside with scraper elements (33) for keeping
the screen openings (32) clear.

The method serves for supplying a pulp suspension (S) to a headbox (1) of a
papermaking or board machine (2) or to a filter device. The pulp suspension (S)
can be formed e.g. by mixing a slush pulp suspension (4) with a diluting liquid
(5). The method uses at least one degassing device (6), the effect of which
corresponds to that of a centrifuge. The method can be implemented in a space-
saving manner and makes it possible e.g. to omit large degassing tanks.

Documents:

01132-kolnp-2007-abstract.pdf

01132-kolnp-2007-claims.pdf

01132-kolnp-2007-correspondence others 1.1.pdf

01132-kolnp-2007-correspondence others 1.2.pdf

01132-kolnp-2007-correspondence others.pdf

01132-kolnp-2007-description complete.pdf

01132-kolnp-2007-drawings.pdf

01132-kolnp-2007-form 1.pdf

01132-kolnp-2007-form 2.pdf

01132-kolnp-2007-form 26.pdf

01132-kolnp-2007-form 3.pdf

01132-kolnp-2007-form 5.pdf

01132-kolnp-2007-international publication.pdf

01132-kolnp-2007-international search report.pdf

01132-kolnp-2007-others.pdf

01132-kolnp-2007-pct others.pdf

01132-kolnp-2007-pct request form 1.1.pdf

01132-kolnp-2007-pct request.pdf

01132-kolnp-2007-priority document.pdf

1132-KOLNP-2007-(07-12-2011)-FORM-27.pdf

1132-KOLNP-2007-(08-08-2012)-FORM-27.pdf

1132-KOLNP-2007-ABSTRACT 1.1.pdf

1132-KOLNP-2007-ABSTRACT.pdf

1132-KOLNP-2007-AMANDED CLAIMS 1.1.pdf

1132-KOLNP-2007-AMANDED CLAIMS.pdf

1132-KOLNP-2007-CORRESPONDENCE 1.1.pdf

1132-KOLNP-2007-CORRESPONDENCE.1.3.pdf

1132-KOLNP-2007-CORRESPONDENCE.pdf

1132-KOLNP-2007-DESCRIPTION (COMPLETE) 1.1.pdf

1132-KOLNP-2007-DESCRIPTION (COMPLETE).pdf

1132-KOLNP-2007-DRAWINGS 1.1.pdf

1132-KOLNP-2007-DRAWINGS.pdf

1132-KOLNP-2007-EXAMINATION REPORT REPLY RECIEVED.pdf

1132-KOLNP-2007-EXAMINATION REPORT.1.3.pdf

1132-KOLNP-2007-FORM 1-1.1.pdf

1132-KOLNP-2007-FORM 1.pdf

1132-KOLNP-2007-FORM 18.1.3.pdf

1132-KOLNP-2007-FORM 2-1.1.pdf

1132-KOLNP-2007-FORM 2.pdf

1132-KOLNP-2007-FORM 26.1.3.pdf

1132-KOLNP-2007-FORM 3.1.3.pdf

1132-KOLNP-2007-FORM 3.pdf

1132-KOLNP-2007-FORM 5.1.3.pdf

1132-KOLNP-2007-FORM 5.pdf

1132-KOLNP-2007-GRANTED-ABSTRACT.pdf

1132-KOLNP-2007-GRANTED-CLAIMS.pdf

1132-KOLNP-2007-GRANTED-DESCRIPTION (COMPLETE).pdf

1132-KOLNP-2007-GRANTED-DRAWINGS.pdf

1132-KOLNP-2007-GRANTED-FORM 1.pdf

1132-KOLNP-2007-GRANTED-FORM 2.pdf

1132-KOLNP-2007-GRANTED-LETTER PATENT.pdf

1132-KOLNP-2007-GRANTED-SPECIFICATION.pdf

1132-KOLNP-2007-OTHERS 1.1.pdf

1132-KOLNP-2007-OTHERS PCT FORM.pdf

1132-KOLNP-2007-OTHERS.1.3.pdf

1132-KOLNP-2007-OTHERS.pdf

1132-KOLNP-2007-PA.pdf

1132-KOLNP-2007-PETITON UNDER RULE 137.pdf

1132-KOLNP-2007-REPLY TO EXAMINATION REPORT.1.3.pdf

abstract-01132-kolnp-2007.jpg


Patent Number 248647
Indian Patent Application Number 1132/KOLNP/2007
PG Journal Number 31/2011
Publication Date 05-Aug-2011
Grant Date 01-Aug-2011
Date of Filing 02-Apr-2007
Name of Patentee VOITH PATENT GMBH
Applicant Address ST. POLTENER STR. 43, 89522 HEIDENHEIM
Inventors:
# Inventor's Name Inventor's Address
1 GOMMEL, AXEL FEDERBURGSTRASSE 107, 88214 RAVENSBURG
2 BINDER, ERWIN OHRINGER WEG 3, 89522 HEIDENHEIM
PCT International Classification Number D21D 5/26
PCT International Application Number PCT/EP05/010094
PCT International Filing date 2005-09-20
PCT Conventions:
# PCT Application Number Date of Convention Priority Country
1 10 2004 051 327.9 2004-10-21 Germany