US3164513A - Distributor system for a paper machine headbox - Google Patents

Distributor system for a paper machine headbox Download PDF

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Publication number
US3164513A
US3164513A US159396A US15939661A US3164513A US 3164513 A US3164513 A US 3164513A US 159396 A US159396 A US 159396A US 15939661 A US15939661 A US 15939661A US 3164513 A US3164513 A US 3164513A
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United States
Prior art keywords
headbox
flow
paper stock
pipes
velocity
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Expired - Lifetime
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US159396A
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English (en)
Inventor
Girard L Calehuff
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West Virginia Pulp and Paper Co
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West Virginia Pulp and Paper Co
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Publication date
Application filed by West Virginia Pulp and Paper Co filed Critical West Virginia Pulp and Paper Co
Priority to US159396A priority Critical patent/US3164513A/en
Priority to FI622245A priority patent/FI45253C/fi
Priority to DE19621411911 priority patent/DE1411911B1/de
Priority to JP37055260A priority patent/JPS498806B1/ja
Priority to GB47244/60A priority patent/GB952158A/en
Priority to SE13483/62A priority patent/SE307289B/xx
Application granted granted Critical
Publication of US3164513A publication Critical patent/US3164513A/en
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

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    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21F—PAPER-MAKING MACHINES; METHODS OF PRODUCING PAPER THEREON
    • D21F1/00—Wet end of machines for making continuous webs of paper
    • D21F1/02—Head boxes of Fourdrinier machines
    • D21F1/024—Details of the feed chamber
    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21F—PAPER-MAKING MACHINES; METHODS OF PRODUCING PAPER THEREON
    • D21F1/00—Wet end of machines for making continuous webs of paper
    • D21F1/02—Head boxes of Fourdrinier machines

Definitions

  • FIG. 2 DISTRIBUTOR SYSTEM FOR A PAPER MACHINE HEADBOX Filed Dec. 14, 1961 G. L. CALEHUFF 2 Sheets-Sheet 2 manna mam FIG. 2
  • This invention relates to new and useful improvements in a method of and an apparatus for distributing a dilute paper stock uniformly across the width of a paper machine headbo-x.
  • the function of a distributor system is to convert the flow of dilute paper stock from flow in a round pipe as is the condition of flow approaching the distributor system to a flow in a rectangular passage extending the width of the headbox as is the condition of the flow leaving the distributor system.
  • the velocity and directionflow of the dilute paper stock must be carefully controlled during the conversion by the distributor system so that the fluid velocity leaving the system is essentially uniform and so that the direction of the flow leaving is everywhere parallel (no crosslows).
  • An ideal distributor system would convert the flow so efiiciently that no further flow eveners would be necessary.
  • the dilute paper stock would flow from the distributor directly onto the paper web former.
  • the velocity profile must be controlled by the distri butor system so that fluctuations or surges in the inlet piping are ineffective in general to the outlet flow and in particular to the slice jet velocity. It is well known in the art of papermaking that flow irregularities remaining in the system after the distributor system in the form of non-uniform velocity profiles, unstable velocity profiles or i non-parallel flow conditions cause undesirable deviations in the physical properties of the finished paper such as varying basis weight profiles and sheet strength due primarily to poor fiber distribution. Since the fluid acted upon by the paper machine distributor system is essentially a forced suspension of solids (wood fibers) in a liquid which will settle or flock together in relatively 'tranquil regions, the distributor system should be a cause of constant mixing and agitation of the dilute paper stock.
  • the stock is introduced into the larger end of the tapered manifold and is forced through the slotted or perforated wall as the stock travels toward the smaller end.
  • the perforated wall does not redirect the dilute paper stock into the headbox properly unless each perforation is "ice accurately designed.
  • alterations to the total flow through the tapered manifold override the design and result in poor stock turning.
  • the fibers carried in the dilute paper stock tend to build up on the perforated plate. Sometimes the fibers are washed off by the flowing force of the dilute paper stock or build up until some of the perforations are completely clogged. Neither effect is desirable.
  • the flocks of fibers that are washed off are not easily, broken up and usually appear in the finished product as a lump or form a thickened area in the paper web which may be picked or removed from the web during passage through various machine components, resulting in a hole in the web and ultimate rejection by the user. Plugging of the perforations by the dilute paper stock obviously reduces the ability of the perforated plate to distribute the dilute paper stock into the headbox evenly thus created a variance in the flow across the headbox and at the slice.
  • the slotted wall does not redirect the dilute paper stock into the headbox in a direction substantially perpendicular to the slice but.
  • the baffles blocked the velocity component that forces the stock toward the wall of the headbox near the small end of the tapered manifold but did not control the direction of the flow between the bafiles; i.e., the flow toward the upper and lower wallsof the headbox.
  • the turning problem associated with the above systems can be substantially reduced by using a row of pipes having a length of between 6 to 10 times the internal diameter.
  • the-pipes, as employed in the prior systems presented problems in blending or mixing the streams from each pipe into a single rectangular stream bounded by the headbox.
  • the eddies acted as the inner and outer walls of an elbow and in the areas containing the eddies, the dilute paper stock was turned and flowed through the slot with little or no kinetic energy change.
  • the overall effect was a varying cross machine flow velocity that ultimately appeared as a differential slice jet velocity.
  • Still others employed a wall having a series of parallel slots that were arranged substantially perpendicular to the inlet end of the manifold. This system, while it would redirect the flow in a direction perpendicular to the inlet flow direction, would not control flow conditions within each slot. The resulting flows may or may not have been parallel and were quite similar in effect to the diffusers discussed above. 7 i
  • Still other manifold systems employed frozen flow conditions where there was little or no turbulence in the dilute paper stock. These systems had inherent cleaning problems and were applied to paper machines of rela tively narrow operating speed ranges and relatively constant stock furnishes.
  • the frozen fiow distributors were usually expensive and difiicult to add to existing headboxes and therefore were not used as improvement additions to existing paper machine headboxes.
  • the principal purpose of this invention is to provide an even and stable velocity flow of dilute paper stock to the headbox regardless of the flow conditions of the feed pipes and to redirect the flow in such a manner that the flow streams are parallel.
  • this invention overcomes the relative complexities present in some of the earlier distributor systems and thereby is adapted to be used as an improvement modification on existing paper machine headboxes.
  • the present invention also has overcome the hydrodynamic problems inherent in the headbox distributor system depending upon impingement and redirection theories for evening the flow such as the explosion type distributor systems.
  • the distributor is applicable to a Wide range of machine speeds and stock furnishes.
  • the dilute paper stock flows from a suitable supply (not shown) into the wider end of the tapered manifold 13.
  • the tapered manifold has a lower wall 22 that slopes gently toward a pipe receiving wall 23.
  • the dilute paper stock is subjected to a flow division wherein a portion flows through the three rows of parallel pipes 19 as the dilute paper stock progresses through the manifold internal area from the larger end toward the smaller end.
  • the lower wall 22 is designed to a slope toward the pipe receiving wall 23 so that the dilute paper stock flowing through the internal area Will be in a zone of relatively constant pressure.
  • each pipe is preferably equally spaced from the nearest pipe, forming a'geometric pattern, wherein each pipe can be imaginarily joinedby straight lines extending from pipe center to pipe center to form a system of equilateral triangles.
  • the pipes in middle row are staggered from the pipes in the outer rows so that the equilateral spacing will occur with the outer rows of pipes being terminated with a pipe 1% located in proximity of each of the corners.
  • the distance from the pipes nearer the edges of the transition wall 24 is preferably approximately half the distance separating the pipes.
  • FIGURE 1 is a sectional elevational view of the distributor system according to a preferred embodiment of this invention, and of a conventional-type headbox and breast roll associated therewith.
  • FIGURE 2 is an elevational view taken along the line 2-2 of FIGURE 1.
  • FIGURE 3 is a sectional view taken along the line 33 of FIGURE 2.
  • FIGURE 4 is a sectional elevational view taken along the line 4-4 of FIGURE 2.
  • the headbox is indicated by the reference 10 and is shown for the purposes of illustration as a pressurized type containing two flow evener rolls 11 for preventing the buildup of minor flow irregularities as the stock travels through the headbox to the slice 12 that feeds the dilute paper stock onto the forming wires 13 at the breast roll 14.
  • the preferred embodiment of the distributor system 15 is angled to the upstream wall'16 of the headbox and extends the width of the headbox.
  • the distributor system 15 is connected to the headbox by the flanges 17 and,
  • the elements in combination provide a distributor system space separating a pipe from an edge of a wall or from another pipe, means the separating distance, or the distance measured from the closest point on the inside surface of a pipe to the closest point on the edge of a wall or on the inside surface of another pipe, as the case may be. From FIGURE 1 and FIGURE 2, notice that the pipes extend substantially perpendicularly away from the transition wall 24 of the headbox inlet chamber and are mutually parallel and equal in length. As indicated in the drawings, the pipes extend perpendicularly along their entire length away from transition wall 24.
  • the headbox inlet chamber 20 is defined by transition wall 24 forming its upstream boundary, inlet tending wall 25 and inlet drive wall 26, which are parallel to each other, two parallel inlet sidewalls 27 and Z8, and the plane between the flanges 1'7 connecting the distribution-system to the headbox, such plane forming the downstream boundary of headbox inlet chamber 2%.
  • the transition wall 24 forms the upstream boundary of the mixing portion 20a of the inlet chamber.
  • the remaining boundaries of the mixing portion of the headbox inlet chamber are formed by the lower portions of inlet tending wall 25, the inlet drive wall 26, and two inlet sidewalls 27 and 28.
  • the lower or impinging surface of the perforated mixing roll 21 forms the downstream boundary of mixing portion Zita.
  • the mixing portion thus defined is the region in which the flow of the dilute paper stock is blended into a single stream covering the cross sectional area of the headbox inlet chamber.
  • the headbox inlet chamber is preferably constant in cross sectional area substantially equal to the cross sectional area of the transition wall 24.
  • the perforated mixing roll 21 has its shaft 30 rotatably held by the bearings 31 so that the lower or impinging surface is in spaced parallel arrangement with the transition wall 24.
  • the mixing roll 21 has a ratio of open to closed area of about 35 percent and is driven by any suitable means which is indicated by the sprocket 32 and chain drive 33.
  • a standard roll used in the industry to even velocity differentials within the headbox performs quite satisfactorily as a mixing roll. By rotating the mixing roll, the possibility of fiber build up on its surfaces is eliminated. A rotative speed of approximately 6 to 10 r.p.m. will prevent fiber build up.
  • FIGURE 4 is illustrative of a means for providing this movement.
  • Two angle members 34 are rigidly attached in spaced, parallel relationship on the inlet tending wall .and the inlet drive wall 26.
  • a hearing block 35 spans the distanceseparating the two angle members and carries the shaft of the perforated mixing roll 21.
  • the bearing block is provided with suitable slots that mate with the angle members 34. The bearing block 35 is held by the slots in such a manner as to limit the movement to a direction of upwardly and downwardly between the angle members 34;
  • a threaded shaft 36 is attached to but rotatably free of the bear-ing block 35.
  • a spacer 37 has internal threading that mates with the threaded shaft 36.
  • the spacer 37 is rigidly attached to the inlet tending wall 25.
  • a pointer 38 is rigidly attached to the bearing block 35.
  • the pointer 38 moves with the bearing block 35 and passes with the bearing block 35 along the graduation-s 39 that are etched or otherwise placed upon the adjacent angle member 34.
  • Inlet walls 25 and 26 contain identical units.
  • the position of the mixing roll can be accurately determined by and repositioned by the relation of the graduations39 with the pointers 3S downstream from the transition wall 24 such that the lower surface of the mixing roll 21 is equally spaced from the pipe outlet ends.
  • the relative slope between i the lower wall 22 and the pipe receiving wall 23 can be designed based on hydrodynamic principles so that the dilute paper stock will be subjected to a zone of equal pressure for a certain value of total flow through the internal area.
  • the design results in a lower wall that is curvilinear and in a manifold that will develop pressure differentials within the internal area whenthe total flow deviates from'the design total flow.
  • a popular practice in the paper industry has been to simplifythe construction and the design .to reduce the cost of the m-anifold by substituting a series of angularly connected straight segments for the curvilinear lower wall.
  • Deviations from the theoretical curvilinear shape of the lower wall resulting from design deficiencies, manufacturing inaccuracies or from the usage of segmented lower walls will cause corresponding pressure variations in the internal area of the tapered manifold.
  • the pressure variations will appear in the prior art distributor systems as velocity differentials in the inlet sections of the headbox and can ultimately appear as velocity differentials at the slice.
  • the tapered manifold used with the distributor system preferably employs a lower wall designed to approach constant internal pressure conditions.
  • the lower wall 22 when used as a part of the distributor system designed according to the invention could be straight without forming detrimental velocities differentials in the slice, even in the absence of a complex flow evening headbox.
  • the shape of the lower Wall 22 is no longer critical when employed in a distributor system designed according to the invention. The underlying reasons for the non-c-ritioality of the heretofore critical shape of the lower wall will be obvious after the important and novel features of the distributor system are explained.
  • the distributor system has incorporated .a novel means for removing the velocity differentials that would normally appear in the headbox and at the slice as a result of the pressure deviations developed by the manifold.
  • Those skilled in. the art of hydrodynamics can reason that the ability of upstream pressure deviations to effect downstream velocities in a fluid can be substantially removed by passing the fluid through a region of high energy loss.
  • the present invention employs a multiplicity of rows of long pipes 19 that have a predetermined energy loss in the form of friction losses to overcome the ability of the pressure deviations developed by the manifolds that result from segmented lower walls,
  • the dilute paper stock leaving each pipe is substantially uniform and equal in velocity.
  • the pipes are employed to overcome another pressure variation that is present in the flow of dilute paper stock, pressure surging. Fluctuations or surges in the pressure of the dilute paper stock delivered to the tapered manifold caused by apparatus located upstream from the manifold, such as a pump, develop random velocity differentials within the headbox and at the slice that vary directly with the square root of the pressure fluctuation or surge. Pipes having relatively small diameters and having considerable lengths as compared W-iththe diameters, effectively control the effect of the pressure surges by decreasing the associated random velocity differentials within the headbox and at the slice. In addition, the ability ofthe pipes to dampen fractional velocity differentials resulting from pressure surges can be increased within limits proportionately with an increase in velocity of the dilute paper stock within the pipes.
  • the pipe length is, within limits, varied directly with the pressure surges developed upstream from the manifold; 'i.e., the pipe length necessary to remove the random velocity differentials within the headbox increases with theamplitude of the pressure surge for constant values of velocity through the pipe-s.
  • the 'pipe'length is varied, within limits, directly with the pressure deviations in the manifold; i.e., the pipe length necessaryy to remove the velocity differentials within the .headbox increases with increases in the pressure deviation. Both effects can usually be rendered ineffective in ability to produce velocity difierenti'als in the headbox by employing pipes having a length of about 3-10 ft.
  • the fibers form a coherent network (fiber plug) in the center of the pipe so that all the change in fluid velocity from average velocity to zero at the pipe wall takes place in an annulus adjacent to the pipe wall. This annulus is usually of very low consistency. This so called plug flow does not allow fiber flocs to be broken up, and hence should be avoided in paper machines.
  • the second regime is obtained by increasing the velocity (V) above that required in the first regime.
  • V velocity
  • the annulus becomes turbulent and begins to destroy the center plug and is often referred to as mixed flow because it consists partly of a fiber plug in the center of the pipe and a turbulent annulus.
  • the presence of the fiber plug infers poor mixing and large flocs both of which are undesirable for the paper maker.
  • the third regime consists of a fully turbulent fiow and hence has the greatest mixing and deflocculation action.
  • the pipes will ordinarily have a length of less than 20 feet, and will perform in the range of 310 feet, which under normal conditions, if the velocity of the dilute paper stock through each pipe is in the range of 5-30 ft./sec., will have sufficient pressure drop (energyloss) to overcome both random and steady state pressure deviations.
  • Commercially clean stainless steel pipes are preferred because there is a minimum tendency of the stock to adhere to the walls.
  • Equal diameter pipeshaving an equal length are preferred which results in an equal pressure drop (energy loss) and velocity through each pipe.
  • the pipe outlet ends are positioned upstream from the mixing roll 21 so that the jets impinge upon the lower surface of the mixing roll.
  • the surface impingement when interrelated with the spacing of the pipes completely mixes and blends the streams into a rectangular flow of substantially equal velocity.
  • the outlet ends of the pipes are positioned relative to one another and to the mixing roll so that the jets of dilute paper stock issuing therefrom will physically and violently interact with one another and form a condition which is preferably described as controlled jet mixing.
  • Optimum impingement conditions are realized when the mixing roll has a ratio of open to closed area in the range of 2050%. A ratio of approximately 35% will perform the jet blending quite satisfactorily..
  • the mixing roll has three distinct and important functions. First, the mixing rollprovides a surface which forces the jets of dilute paper stock to blend in a controlled uniform manner before they have an opportunity to establish an uneven flow pattern. Second, the energy conversion is obtained without subjecting the dilute paper stock to over-expansion and redirectional flow paths, removing the possibility of forming uncontrollable turbulence that is inherent in systems containing redirecting chambers. Third, the mixing roll subjects the stock to an additional velocity evening zone which is contained Within the internal area of the mixing roll further equalizing the velocity profile in the distributor system. Referring to FIGURE 1 of the drawings, notice that the flow of dilute paper stock in the distributorsystem is subjected to only one turning which occurs at the entrance ends of the pipes.
  • the flows ofdilute paper stock is thereafter substantially straight and is contained within the headbox inlet chamber which is preferably constant in cross sectional area.
  • the distributor system has. completely removed the possibility of any uncontrollable, unpredictable, or unpredeterminable turbulence, secondary eddies, or velocity differentials that are present in distributor' systems subjecting the flow to multiple turning conditions, and has removed the possibiblity of over-expanding the dilute paper stock after mixing and blending.
  • the mixing roll should be separated from the outlet ends of the pipes by approximately five inches and not more than approximately 20 inches. Experience has shownthat 12 inches is workable in most cases. The exact location is best determined by adjusting the position of the mixing roll and observing the reaction of the slice jet velocity.
  • FIGURE 4 of the drawings is indicative of an adjusting device.
  • a distributor system of the type described herein is necessarily complex to design properly because of the number of factors that must be taken into account, all of which are decidedly important, but some of which are necessarily dependent upon more controlling factors.
  • the following discussion deals with a design procedure which is felt to be desirable.
  • the design procedure can be affected by conditions that vary from paper machine to paper machine. As an example, adding the distributor system to existing paper machines sometimes develops space limitations, and requires increasing the available pumping head.
  • the design can be determined by knowing the flow at which the paper machine will be running the majority of the time.
  • the width of the paper machine is related to the total flow of dilute paper stock to determine the size of the manifold.
  • a flow velocity and a pipe diameter for each pipe is chosen so that the flow through each pipe is fully turbulent (has 21 Reynolds number of at least 10 thus creatiing deflocculation conditions within the pipe.
  • Pipe diameter and velocity are divided into the total flow to determine the number of pipes necessary.
  • the number of pipes are physically deployed to obtain proper mixing and to prevent over-expansion.
  • the number of rows of pipes is decided upon, usually an odd number is preferred so that the deployment is as described earlier.
  • the size of the transition wall 24 is determined by the pipe deployment, with the exception of the length which is determined by the width of the paper machine.
  • the length of the pipes is determined based on the aforesaid principles that the ability of pressure deviations to cause velocity differentials is inversely proportional to the energy loss. An energy loss of 2-5 ft. of water in the pipes will usually overcome the pressure deviations.
  • the position of the mixing roll is determined.
  • the mixing roll should have an outside diameter just slightly less than the depth of the mixing portion of the headbox inlet chamber and a length substantially equal to the width of the headbox inlet chamber.
  • the distributor system when designed according to this invention will effectively block upstream disturbances including manifold inaccuracies resulting in stable and uniform flows of dilute paper stock through the headbox. It should be realized that many modifications and variations are possible that are still within the scope of this invention.
  • a distributor system for delivering dilute paper stock uniformly to a paper machine headbox comprising:
  • a headbox inlet chamber extending the width of the headbox and opening into the headbox along the full width thereof, and having a transition wall extending the width of the headbox and forming the upstream boundary of said headbox inlet chamber opposite said opening, all cross-sectional areas of said headbox inlet chamber measured in any plane therein parallel to the said transition wall and perpendicular to the direction of flow of dilute paper stock therethrough being substantially equal to each other and substantially equal to the area outlined by the boundaries of said transition wall,
  • a tapered manifold extending the full length of the said headbox inlet chamber and having a wall receiving the inlet ends of said pipes and an opening at its wider end for receiving the dilute paper stock.
US159396A 1961-12-14 1961-12-14 Distributor system for a paper machine headbox Expired - Lifetime US3164513A (en)

Priority Applications (6)

Application Number Priority Date Filing Date Title
US159396A US3164513A (en) 1961-12-14 1961-12-14 Distributor system for a paper machine headbox
FI622245A FI45253C (fi) 1961-12-14 1962-12-13 Menetelmä laimean paperimassalietteen virtauksen saamiseksi yhdenmukai seksi paperikoneen jakolaatikon koko leveydellä ja laite tämän menetel män suorittamiseksi.
DE19621411911 DE1411911B1 (de) 1961-12-14 1962-12-13 Stoffauflauf fuer Papiermaschinen
JP37055260A JPS498806B1 (de) 1961-12-14 1962-12-14
GB47244/60A GB952158A (en) 1961-12-14 1962-12-14 Method and apparatus for evening the flow of paper to a paper machine headbox
SE13483/62A SE307289B (de) 1961-12-14 1962-12-14

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
US159396A US3164513A (en) 1961-12-14 1961-12-14 Distributor system for a paper machine headbox

Publications (1)

Publication Number Publication Date
US3164513A true US3164513A (en) 1965-01-05

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ID=22572443

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Application Number Title Priority Date Filing Date
US159396A Expired - Lifetime US3164513A (en) 1961-12-14 1961-12-14 Distributor system for a paper machine headbox

Country Status (6)

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US (1) US3164513A (de)
JP (1) JPS498806B1 (de)
DE (1) DE1411911B1 (de)
FI (1) FI45253C (de)
GB (1) GB952158A (de)
SE (1) SE307289B (de)

Cited By (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3272233A (en) * 1963-03-08 1966-09-13 Diamond Int Corp Taper flow inlet
US3385754A (en) * 1965-02-11 1968-05-28 West Virginia Pulp & Paper Co Stock distribution system
US3887429A (en) * 1972-03-08 1975-06-03 Lonza Ag Device for untangling and dispersing fibrous materials
US4464225A (en) * 1979-10-08 1984-08-07 Bell Maschinenfabrik Ag Method and machine for fabricating building boards
US5277765A (en) * 1992-06-18 1994-01-11 Voith, Inc. Headbox with a vertical partition between perforated rolls
US5423948A (en) * 1992-06-18 1995-06-13 Voith Sulzer Paper Technology North America, Inc. Headbox with a vertical partition between perforated rolls
US5575559A (en) * 1994-09-19 1996-11-19 Goulds Pumps, Inc. Mixer for mixing multi-phase fluids
US6413376B1 (en) 1998-02-09 2002-07-02 United States Gypsum Company Headbox for gypsum/fiber board production
US6457974B1 (en) * 1999-11-18 2002-10-01 Parkell, Inc. Intraoral dental abrading instrument
CN102373640A (zh) * 2011-10-17 2012-03-14 上海伊索热能技术有限公司 一种匀浆辊及其使用该匀浆辊进行匀浆的方法

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2688276A (en) * 1951-05-11 1954-09-07 Marathon Corp Head box for paper machines
US2737087A (en) * 1950-04-25 1956-03-06 Int Paper Canada Headbox for paper machine
US2929449A (en) * 1955-08-22 1960-03-22 Auglo Paper Products Ltd Fluid flow distribution devices
US3055421A (en) * 1958-03-07 1962-09-25 Rice Barton Corp Stock inlet

Family Cites Families (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE853256C (de) * 1950-04-25 1952-10-23 Canadian Internat Paper Compan Verfahren und Geraet zur Aufbereitung der Stoffaufschlemmung, die vom Stoffauflaufkasten auf das Sieb einer Papiermaschine gefoerdert wird
US2911041A (en) * 1956-12-27 1959-11-03 Beloit Iron Works Stock distributor assembly
US2894581A (en) * 1957-03-26 1959-07-14 Rice Barton Corp Fluid stock distributor
US3010510A (en) * 1958-01-23 1961-11-28 Rice Barton Corp Slice control mechanism
FR1252331A (fr) * 1960-03-14 1961-01-27 Beloit Iron Works Distributeur de matière à tubes multiples

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2737087A (en) * 1950-04-25 1956-03-06 Int Paper Canada Headbox for paper machine
US2688276A (en) * 1951-05-11 1954-09-07 Marathon Corp Head box for paper machines
US2929449A (en) * 1955-08-22 1960-03-22 Auglo Paper Products Ltd Fluid flow distribution devices
US3055421A (en) * 1958-03-07 1962-09-25 Rice Barton Corp Stock inlet

Cited By (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3272233A (en) * 1963-03-08 1966-09-13 Diamond Int Corp Taper flow inlet
US3385754A (en) * 1965-02-11 1968-05-28 West Virginia Pulp & Paper Co Stock distribution system
US3887429A (en) * 1972-03-08 1975-06-03 Lonza Ag Device for untangling and dispersing fibrous materials
US4464225A (en) * 1979-10-08 1984-08-07 Bell Maschinenfabrik Ag Method and machine for fabricating building boards
US5277765A (en) * 1992-06-18 1994-01-11 Voith, Inc. Headbox with a vertical partition between perforated rolls
US5423948A (en) * 1992-06-18 1995-06-13 Voith Sulzer Paper Technology North America, Inc. Headbox with a vertical partition between perforated rolls
US5575559A (en) * 1994-09-19 1996-11-19 Goulds Pumps, Inc. Mixer for mixing multi-phase fluids
US6413376B1 (en) 1998-02-09 2002-07-02 United States Gypsum Company Headbox for gypsum/fiber board production
US6605186B2 (en) 1998-02-09 2003-08-12 United States Gypsum Company Headbox for gypsum/fiber board production
US6457974B1 (en) * 1999-11-18 2002-10-01 Parkell, Inc. Intraoral dental abrading instrument
CN102373640A (zh) * 2011-10-17 2012-03-14 上海伊索热能技术有限公司 一种匀浆辊及其使用该匀浆辊进行匀浆的方法
CN102373640B (zh) * 2011-10-17 2014-04-02 上海伊索热能技术有限公司 一种利用匀浆辊进行匀浆的方法

Also Published As

Publication number Publication date
JPS498806B1 (de) 1974-02-28
DE1411911B1 (de) 1970-02-26
FI45253C (fi) 1972-04-10
FI45253B (de) 1971-12-31
GB952158A (en) 1964-03-11
SE307289B (de) 1968-12-23

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