US3496261A - Distribution of viscous liquid substances in pipes - Google Patents

Distribution of viscous liquid substances in pipes Download PDF

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Publication number
US3496261A
US3496261A US352786A US35278664A US3496261A US 3496261 A US3496261 A US 3496261A US 352786 A US352786 A US 352786A US 35278664 A US35278664 A US 35278664A US 3496261 A US3496261 A US 3496261A
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Prior art keywords
pipe
spinning
liquid
station
manifold
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US352786A
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William Geoffrey Parr
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    • D—TEXTILES; PAPER
    • D01—NATURAL OR MAN-MADE THREADS OR FIBRES; SPINNING
    • D01D—MECHANICAL METHODS OR APPARATUS IN THE MANUFACTURE OF ARTIFICIAL FILAMENTS, THREADS, FIBRES, BRISTLES OR RIBBONS
    • D01D1/00—Treatment of filament-forming or like material
    • D01D1/06—Feeding liquid to the spinning head
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10T—TECHNICAL SUBJECTS COVERED BY FORMER US CLASSIFICATION
    • Y10T137/00—Fluid handling
    • Y10T137/0318—Processes
    • Y10T137/0324—With control of flow by a condition or characteristic of a fluid
    • Y10T137/0363—For producing proportionate flow
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10T—TECHNICAL SUBJECTS COVERED BY FORMER US CLASSIFICATION
    • Y10T137/00—Fluid handling
    • Y10T137/2496—Self-proportioning or correlating systems
    • Y10T137/2559—Self-controlled branched flow systems
    • Y10T137/265—Plural outflows
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10T—TECHNICAL SUBJECTS COVERED BY FORMER US CLASSIFICATION
    • Y10T137/00—Fluid handling
    • Y10T137/8593—Systems
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10T—TECHNICAL SUBJECTS COVERED BY FORMER US CLASSIFICATION
    • Y10T137/00—Fluid handling
    • Y10T137/8593—Systems
    • Y10T137/85978—With pump
    • Y10T137/86131—Plural
    • Y10T137/86163—Parallel

Definitions

  • each spinning head may be individually supplied by a pipe leading directly to it from the melter.
  • a number of spinning heads may be fed from each of one or more pipes, and such pipes may or may not circulate some of the polymer back into the melter.
  • the molten polymer has to be supplied under a pressure suflicient to ensure its uniform flow in sufficient quantity down the pipe or pipes in question; and in this regard there are clear advantages, due to the lesser pressure required for a given transit time, and due to the simplicity of the pipework and the means for holding it at the required high temperature, in supplying a given number of spinning heads from a common pipe than in supplying them by individual pipes.
  • This invention is concerned with the supply of viscous liquid material, such as the molten polymer material above referred to, to a number of positions by means of a single distribution pipe.
  • melt-spinning system in which one melter supplies a number of spinning heads, it is important to try and ensure that each spinning head is supplied with polymer that has taken the same average time to travel on its way from the melter.
  • the mean transit times of the polymer streams to be extruded from each head shall be as near equal as possible.
  • melt-spinning materials such as nylon, degrade and change their physical and chemical properties when kept at the high temperatures necessary to ensure fluidity.
  • the supplies to different spinning positions must be, if not negligibly degraded, at least substantially equally degraded.
  • the mean transit time of the polymer at each section is dependent on the length of pipe down which the polymer has travelled; the longer the flow path, the longer the mean transit time and the greater the degradation in the polymer at that section.
  • the invention comprises a process for providing a vis- 3,496,261 Patented Feb. 17, 1970 ice cons liquid material under pressure from a source thereof along a pipe to a plurality of positions, e.g. spinning heads, in which process successive positions or groups of positions up to the final position or group of positions are supplied from stations along the pipe at each of which an outer annular portion containing the liquid required by its position or positions is withdrawn from the approaching stream and in which the final position or positions is or are supplied from the end of the pipe, the internal dimensions of the pipe along its length and the spacing of the stations being such that the mean times of transit of the liquid material from the inlet of the pipe to each of the positions are substantially equal.
  • positions e.g. spinning heads
  • apparatus comprises liquid withdrawal means provided at a station or stations along a pipe through which pipe viscous liquid material is adapted to flow from a source of supply thereof, such means being adapted to withdraw from the approaching stream an outer annular portion containing the amount of liquid required at any such station for the supply of a position or group of positions, e.g. spinning heads, supplied from said station, the successive lengths and internal cross-sectional areas of the pipe between the inlet and the first of such stations, between any two such stations, and between the final such station and the downstream end of the pipe itself, being so selected, as by step-wise or gradual variations in the size of cross-section, that the mean times of transit of the liquid material from the inlet of the pipe to each of the positions are substantially equal.
  • the mean times of transit referred to herein are the arithmetic means of the several times of transit.
  • the dimensions of the pipe may be chosen to give a set of different mean transit times.
  • the invention equally comprehends an arrangement whereby the direction of flow is reversed, moving from the several sources of supply to a common outlet.
  • meter pumps e.g. gear pumps
  • Another important consequence of the invention is that, as none of the material flowing very slowly close to the Walls of the pipe has to travel further than the distance between two tapping stations, little will remain in the pipe for long enough to gel, which some polymeric materials have a tendency to do when kept in molten condition for any appreciable length of time. Certainly, there is a great improvement over the amount of longdwelling polymer that is present in a com-parable direct feed down an individual pipe.
  • the pipe is required to distribute equal quantities of molten polymer material to each of four spinning heads with equal mean transit times, and the volume of section between the inlet and the first tapping station is V, then the volume of the section between the first and second stations will be 0.5V, that of the section between the second and third stations 031V, and that between the third station and the end of the pipe 0.19V. It can be calculated that, if the sections are themselves of equal length, and the final pump is at a given fixed distance from the supply, then the pressure required in a system as above described will be only a quarter that required to distribute the same material, with the same equal mean transit times, by means of individual pipes. Further, at each of the spinning heads of the system, there will be far less of the polymer material that has moved very slowly and hence has a significantly long transit time, than will be the case if individual pipes are used, achieving the same throughputs.
  • FIGURE 1 is a diagram showing a molten synthetic polymer distribution pipe with four positions fed there from, according to the invention:
  • FIGURE 2 is a diagram showing the essential features of one embodiment of a twin-branch tapping station (or stripping junction) for use in the invention
  • FIGURE 3 is a diagrammatic sectional view of one design of a singlebranch tapping station (or stripping junction) for use in the invention, in which division of the stream of liquid takes place upstream of the branch position;
  • FIGURE 4 is a diagrammatic sectional view of another design of a single-branch tapping station( or stripping junction) for use in the invention, in which division of the stream takes place downstream of the branch position;
  • FIGURE 5 is a diagrammatic sectional view of a design of a single-branch tapping station (or stripping junction) for use in the invention, which station incorporates an annual metering slot and a plenum chamber;
  • FIGURE 6 is a variant of the design of FIGURE 5, for a twin-branch tapping station (or stripping junction);
  • FIGURE 7 is a digram of a four branch tapping station (or stripping junction) for use in the invention.
  • FIGURE 8 is a graph of the distribution (or spread) of transit times of liquid at each of three positions, compared with that of liquid at the end of a pipe of volume equal to that occupied by any one of the streams leading to such positions.
  • a polymer distribution manifold M leading from a source of supply such as the melter or polymeriser of a melt-spinning unit (not shown) consists of a pipe having three step-wise reductions in diameter at tapping stations (or stripping junctions) T T and T
  • the manifold is thus divided, as shown, into four sections along its length.
  • successive tapping stations T T and T strip from the approaching stream outer annuli of molten polymer each containing one quarter of the input to the pipe and direct them to positions (spinning heads) P P and P respectively.
  • the residual core of molten polymer proceeds along the final (fourth) section of the manifold directly to position P
  • the flows to the spinning heads are controlled by meter pumps G which are gang driven as indicated by the dashed line D.
  • the volumetric flow, a is the same, and is a quarter that of the input, 4a, of the manifold.
  • the dotted lines within the manifold show the boundaries between the streams flowing to the respective positions.
  • FIGURE 2 three branches B B and B are fed with equal volumetric flows from manifold M.
  • the tapping station T is a simple twin-branch junction.
  • This figure shows the upstream end portion of the smaller diameter pipe of branch B protruding concentrically backwardly into the downstream end portion of the manifold M.
  • Such backward protrusion of the inner pipe, and the width of the annual gap between the two pipes, are important factors related to the stripping efficiency of the junction.
  • the longer the protruding length of the inner pipe the better the stripping eificiency; but, on the other hand, the longer the protruding length, the greater will be the spread of transit times for the liquid in the annular gap. Hence, a compromise is necessary, to achieve the optimum performance for the liquid in question, in the particular process.
  • the tapping station T on manifold M is a single stripping junction, having branch pipe, B.
  • division of the stream takes place upstream of the junction, as also shown in FIGURE 2, by virtue of the backward protrusion of the inner pipe of the stepped-down portion of the manifold within the larger-diameter upstream portion of the manifold.
  • division of the stream takes place downstream of the branch, B, the outer annulus of the stream of liquid being reversed in direction before flowing down the branch pipe.
  • Such downstream division of the stream may have advantages over the other method, in that the slower-moving liquid of the manifold, close to its walls, is directed into the centre of the branch pipe, and hence the spread of transit times at the outlet of the branch (e.g. a spinning head) is reduced; and in that the length of the last section of the manifold, where most of the pressure drop of the -entire manifold takes place, is reduced and hence the total pressure drop can be reduced or a lower mean transit time for the same pressure drop achieved.
  • FIGURES 5 and 6 illustrate the use of an annular metering slot at the tapping point leading to an annular plenum chamber, C.
  • FIGURE 6 being an example of a multi-branch junction, the presence of a sufiiciently large plenum chamber would enable the asymetric arrangement of branch pipes B and B should this be desired.
  • branch pipes B B B and B are of equal diameter to that of manifold M, such that they more than cover the circumference of the manifold at the tapping station, T, which overlap is necessary if proper stripping of the entire outer annulus, as required, is to take place by means of the action of meter pumps extracting an equal flow in each of the branch pipes.
  • the graph of FIGURE 8 readily indicates the equivalence of the distributions of transit times of three outlet positions from a manifold constructed according to 'the invention, and compares these three curves with one for a simple pipe of equivalent volume.
  • the unit of the abscissa is time t minutes, and that of the ordinate is the percentage of liquid with a transit time greater than t minutes.
  • the apparatus used for obtaining the values to be plotted for the curves of the manifold outlets was one comprising three outlet positions, two such positions being fed from successive single-branch tapping stations along the length of the manifold and one position being fed directly from the end section of the manifold.
  • the apparatus was designed to give equal mean transit times for the streams to the three outlet positions, when the flows from the three outlets were equal.
  • a throughput of 30 cc./min. of viscous liquid material at each outlet was used in the tests.
  • the volume occupied by each of the three streams of liquid was 237 cc.
  • the dimensions of the three sections of the manifold were, respectively, from the input end:
  • molten polymeric material for example molten polyhexamethylene adipamide
  • Such homogenising will be desirable when nonuniform degradation occurs in the melter or polymeriser supplying polymeric material to the manifold pipe, and it may be necessary in the branch lines so as to mix the laminae flowing into each line and thus to prevent unevenly degraded polymer from being supplied across the face of the spinneret with the consequent extrusion of poorer filaments from some holes than others.
  • the type of tapping station shown in FIGURE 4 is conducive to this end.
  • the pipe is usually of progressively stepped-down diameter, and this is convenient since it is usual to wish to have the various sections of the pipe between tappings of equal length, it is not strictly necessary, according to our invention, for the pipe to be so proportioned. It is only essential that the volumes of the various sections between tappings shall be such as to give the equal mean transit times, or such other ratio of transit times as may be required. And hence, if the lengths of the various sections can be, and are, made unequal to the extent necessary to give the required volumes, the cross-section of the pipe can, in fact, be constant throughout the length of the pipe.
  • a process for melt spinning synthetic polymeric material said process being of the type including providing viscous liquid synthetic polymeric material under pressure from a source thereof to the inlet of a pipe, providing a succession of stations along the pipe, providing a succession of spinning positions with at least one position correspoding to each station and with at least one of the last positions in the succession corresponding to the end of the pipe, collecting at each station an outer annular portion of the liquid material approaching the station, conducting the collected portion to each spinning position associated therewith in the amount required by the spinning position and conducting liquid material from the downstream end of the pipe to each spinning position associated therewith in the amount required by the spinning position, the improvement which comprises receiving the conducted liquid material into a meter pump at each spinning position, pumping the received liquid material to a spinning head associated with the spinning position, said pumping operation delivering liquid material to all of the spinning heads at the same flow rate and establishing substantial equality of residence times of the liquid material travelling from the inlet of the pipe to each spinning position solely by selection of the dimensions of the pipe along its length.
  • a process as in claim 1 including homogenising the liquid material being conducted from the pipe to the positions for the purpose of preventing unevenly degraded polymeric material from reaching the spinning heads.
  • step of selecting the dimensions of the pipe includes selecting the successive lengths and internal cross-sectional areas of the pipe between the inlet end and the first of the stations, between successive stations, and between the final station and the downstream end of the pipe.
  • a manifold pipe for the distribution of molten synthetic polymer material to a plurality of spinning heads from a source of such material, said pipe having at least one stripping junction along its length from which at least one branch pipe leads to a spinning head and havig an end section leading directly to at least one spinning head, said stripping junction or junctions being adapted to direct an outer annular portion of the molten material from the approaching stream into said branch pipe or pipes, and each of said spinning heads being provided with a meter pump to control the amount of molten material supplied to each head, the dimensions of the manifold pipe along its length being such that the mean times of transit of the molten material from the inlet of the pipe to each of the spinning heads are substantially equal.
  • stripping junction or each of the stripping junctions comprises an upstream end portion of a section of the pipe of smaller diameter protruding backwardly and concentrically into the downstream end portion of the immediately preceding section of the pipe of larger diameter.
  • a manifold pipe as claimed in claim 9 in which there is a single branch pipe leading from each stripping junction.
  • a manifold pipe as claimed in claim 5 in which the stripping junction or each of the stripping junctions 5 comprises an annular metering slot leading, into an annular plenum chamber.
  • a manifold pipe as claimed in claim 11 in which a plurality of branch pipes are asymmetrically spaced around and lead from the annular plenum chamber.

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • Textile Engineering (AREA)
  • Spinning Methods And Devices For Manufacturing Artificial Fibers (AREA)
  • Extrusion Moulding Of Plastics Or The Like (AREA)
US352786A 1963-03-22 1964-03-18 Distribution of viscous liquid substances in pipes Expired - Lifetime US3496261A (en)

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Application Number Priority Date Filing Date Title
GB11378/63A GB1012501A (en) 1963-03-22 1963-03-22 Improvements in or relating to the distribution of viscous liquid substances in pipes

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US (1) US3496261A (de)
BE (1) BE645525A (de)
CH (1) CH417840A (de)
DE (1) DE1435359C3 (de)
GB (1) GB1012501A (de)
LU (1) LU45715A1 (de)
NL (1) NL6402994A (de)
SE (1) SE303825B (de)

Cited By (19)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3640308A (en) * 1970-04-15 1972-02-08 Du Pont Apparatus for dividing and recombining flow
US3800985A (en) * 1971-04-15 1974-04-02 Kenics Corp System and method for distributing highly viscous molten material
US4007247A (en) * 1972-09-26 1977-02-08 Imperial Chemical Industries Limited Production of fibrils
US4682710A (en) * 1986-04-15 1987-07-28 Nordson Corporation Multi-station viscous liquid distribution system
US4682711A (en) * 1985-04-08 1987-07-28 Nordson Corporation Method and apparatus for sealing welded seams of automobiles
US4688590A (en) * 1985-07-12 1987-08-25 Bayer Aktiengesellschaft Process and an apparatus for the distribution of fluids
US4706885A (en) * 1984-08-06 1987-11-17 Morin Rolland L Liquid distribution system
US4761343A (en) * 1985-09-13 1988-08-02 Gellert Jobst U Injection molding manifold system having balanced bridging manifold
US4782857A (en) * 1986-02-07 1988-11-08 Sulzer Brothers Limited Method and apparatus for uniformly distributing solids-containing liquid
US4818384A (en) * 1987-08-14 1989-04-04 Mayer Robert B Recirculating sand filter
US4822485A (en) * 1987-08-14 1989-04-18 Mayer Robert B Recirculating sand filter valve
US4993454A (en) * 1983-12-16 1991-02-19 Hitachi, Ltd. Piping branch structure
US5066444A (en) * 1990-07-05 1991-11-19 Dowbrands Inc. Process and apparatus for reducing color contamination in the process recycle of zippered thermoplastic bags
US5165450A (en) * 1991-12-23 1992-11-24 Texaco Inc. Means for separating a fluid stream into two separate streams
US5651928A (en) * 1994-04-21 1997-07-29 Basf Corporation Process for melt mixing and spinning synthetic polymer
US5794642A (en) * 1995-07-26 1998-08-18 Lenzing Aktiengesellschaft Process for transporting thermally unstable viscous masses
US5911155A (en) * 1992-08-03 1999-06-08 Environ Products, Inc. Connecting device for pipe assemblies
US20070063374A1 (en) * 2004-11-08 2007-03-22 Nicholas Barakat System and method for making polyethylene terephthalate sheets and objects
US9011737B2 (en) 2004-11-08 2015-04-21 Chemlink Capital Ltd. Advanced control system and method for making polyethylene terephthalate sheets and objects

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB2208904A (en) * 1987-08-20 1989-04-19 Tankmaster Ltd Adaptor for tank contents gauge
GB9025829D0 (en) * 1990-11-28 1991-01-09 Shell Int Research Apparatus for dividing a stream of multi-phase fluid

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US699079A (en) * 1901-10-15 1902-04-29 Joseph Coles Water distribution.
US2599680A (en) * 1947-08-26 1952-06-10 Curtiss Wright Corp Liquid distributing system
US3000053A (en) * 1959-01-26 1961-09-19 Eastman Kodak Co Melt spinning
US3034526A (en) * 1959-11-13 1962-05-15 Du Pont Laminar fluid flow process
US3103942A (en) * 1961-09-22 1963-09-17 Du Pont Apparatus and process for distributing viscous liquids

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US699079A (en) * 1901-10-15 1902-04-29 Joseph Coles Water distribution.
US2599680A (en) * 1947-08-26 1952-06-10 Curtiss Wright Corp Liquid distributing system
US3000053A (en) * 1959-01-26 1961-09-19 Eastman Kodak Co Melt spinning
US3034526A (en) * 1959-11-13 1962-05-15 Du Pont Laminar fluid flow process
US3103942A (en) * 1961-09-22 1963-09-17 Du Pont Apparatus and process for distributing viscous liquids

Cited By (24)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3640308A (en) * 1970-04-15 1972-02-08 Du Pont Apparatus for dividing and recombining flow
US3800985A (en) * 1971-04-15 1974-04-02 Kenics Corp System and method for distributing highly viscous molten material
US4007247A (en) * 1972-09-26 1977-02-08 Imperial Chemical Industries Limited Production of fibrils
US4993454A (en) * 1983-12-16 1991-02-19 Hitachi, Ltd. Piping branch structure
US4706885A (en) * 1984-08-06 1987-11-17 Morin Rolland L Liquid distribution system
US4682711A (en) * 1985-04-08 1987-07-28 Nordson Corporation Method and apparatus for sealing welded seams of automobiles
US4688590A (en) * 1985-07-12 1987-08-25 Bayer Aktiengesellschaft Process and an apparatus for the distribution of fluids
US4761343A (en) * 1985-09-13 1988-08-02 Gellert Jobst U Injection molding manifold system having balanced bridging manifold
US4782857A (en) * 1986-02-07 1988-11-08 Sulzer Brothers Limited Method and apparatus for uniformly distributing solids-containing liquid
US4682710A (en) * 1986-04-15 1987-07-28 Nordson Corporation Multi-station viscous liquid distribution system
US4818384A (en) * 1987-08-14 1989-04-04 Mayer Robert B Recirculating sand filter
US4822485A (en) * 1987-08-14 1989-04-18 Mayer Robert B Recirculating sand filter valve
US5066444A (en) * 1990-07-05 1991-11-19 Dowbrands Inc. Process and apparatus for reducing color contamination in the process recycle of zippered thermoplastic bags
US5165450A (en) * 1991-12-23 1992-11-24 Texaco Inc. Means for separating a fluid stream into two separate streams
US5911155A (en) * 1992-08-03 1999-06-08 Environ Products, Inc. Connecting device for pipe assemblies
US6029505A (en) * 1992-08-03 2000-02-29 Environ Products, Inc. Connecting device for pipe assemblies
US5651928A (en) * 1994-04-21 1997-07-29 Basf Corporation Process for melt mixing and spinning synthetic polymer
US5656304A (en) * 1994-04-21 1997-08-12 Basf Corporation Apparatus for melt mixing and spinning synthetic polymers
US5697402A (en) * 1994-04-21 1997-12-16 Basf Corporation Apparatus for melt mixing synthetic polymers
US5794642A (en) * 1995-07-26 1998-08-18 Lenzing Aktiengesellschaft Process for transporting thermally unstable viscous masses
US20070063374A1 (en) * 2004-11-08 2007-03-22 Nicholas Barakat System and method for making polyethylene terephthalate sheets and objects
US8545205B2 (en) * 2004-11-08 2013-10-01 Chemlink Capital Ltd. System and method for making polyethylene terephthalate sheets and objects
US8986587B2 (en) 2004-11-08 2015-03-24 Chemlink Capital System and method for making polyethylene terephthalate sheets and objects
US9011737B2 (en) 2004-11-08 2015-04-21 Chemlink Capital Ltd. Advanced control system and method for making polyethylene terephthalate sheets and objects

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Publication number Publication date
CH417840A (fr) 1966-07-31
DE1435359B2 (de) 1973-02-22
LU45715A1 (de) 1964-05-21
NL6402994A (de) 1964-09-23
SE303825B (de) 1968-09-09
BE645525A (de) 1964-09-21
DE1435359C3 (de) 1975-10-02
DE1435359A1 (de) 1969-05-08
GB1012501A (en) 1965-12-08

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