US2355057A - Apparatus for deaerating viscose compositions - Google Patents

Apparatus for deaerating viscose compositions Download PDF

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Publication number
US2355057A
US2355057A US403007A US40300741A US2355057A US 2355057 A US2355057 A US 2355057A US 403007 A US403007 A US 403007A US 40300741 A US40300741 A US 40300741A US 2355057 A US2355057 A US 2355057A
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United States
Prior art keywords
viscose
tank
vacuum
temperature
air
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Expired - Lifetime
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US403007A
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English (en)
Inventor
Norman A Copeland
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EIDP Inc
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EI Du Pont de Nemours and Co
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Publication date
Application filed by EI Du Pont de Nemours and Co filed Critical EI Du Pont de Nemours and Co
Priority to US403007A priority Critical patent/US2355057A/en
Priority to GB6952/44A priority patent/GB564153A/en
Priority to GB9909/42A priority patent/GB561050A/en
Application granted granted Critical
Publication of US2355057A publication Critical patent/US2355057A/en
Priority to FR927413D priority patent/FR927413A/fr
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

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Classifications

    • 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
    • D01D1/10—Filtering or de-aerating the spinning solution or melt
    • D01D1/103—De-aerating
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D19/00—Degasification of liquids
    • B01D19/0021—Degasification of liquids by bringing the liquid in a thin layer
    • D—TEXTILES; PAPER
    • D01—NATURAL OR MAN-MADE THREADS OR FIBRES; SPINNING
    • D01F—CHEMICAL FEATURES IN THE MANUFACTURE OF ARTIFICIAL FILAMENTS, THREADS, FIBRES, BRISTLES OR RIBBONS; APPARATUS SPECIALLY ADAPTED FOR THE MANUFACTURE OF CARBON FILAMENTS
    • D01F2/00—Monocomponent artificial filaments or the like of cellulose or cellulose derivatives; Manufacture thereof
    • D01F2/06—Monocomponent artificial filaments or the like of cellulose or cellulose derivatives; Manufacture thereof from viscose
    • D01F2/08—Composition of the spinning solution or the bath
    • 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
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S159/00—Concentrating evaporators
    • Y10S159/31—Deaeration

Definitions

  • the present invention relates to apparatus for the removal of air, or other gases, contained in liquids. More specifically, it' relates to the removal of air and other gases from viscose in a continuous manner.
  • Air is present in viscose in two forms, that is, as occluded air which appears as bubbles and dissolved air. If a body of viscose is subjected to a vacuum, the bubbles present becomes larger becauseof the decreased pressure and tendto rise more rapidly tothe surface. The dissolved air forms bubbles and gradually comes out of solution at the surface of the viscose. These actions, of course, become faster the thinner the If a film of viscose is passed continuously over a vertical surface, the same actions take place, but at any reasonable filmvelocity, under low vacuum, i.
  • the viscose may be passed through a series of rest tanks under this high vacuum. It is further'known to cause the viscose to be spread in a thin film in a container and to subject it to a vacuum which preferably does not cause boiling of the viscose.
  • This chamber is preferably so designed that all wetted portions of said chamber are washed by a continuous flow of viscose and that sputtering of the boiling solution on dry portionsof the chamber is substantially eliminated, thereby substantially preventing the vacuum in the chamber,
  • the bulb transmits ture reading to the temperature gauge 5
  • Similar temperature bulb 53 Preferably, the temperature differential between the incomingviscose and the boiling point of the viscose is maintained constant byregulatwhereby .the quantity of water eve-ported per unit volume of viscose will remain substantially constant.
  • Figure l is a vertical sectional view of a deaerating apparatus suitable for use in accordance with the present invention.
  • Figure 2 is a top plan view of the apparatus shown in Figure l.
  • Figure 3 is an enlarged sectional view showing a detail of the viscose distributing device of the deaeration apparatus.
  • Figure 4 is an enlarged sectional view. of a modified form of distributor device.
  • Figure 5 is a diagrammatic elevational: view, in section, of a modified form of deaeration apparatus constructed in accordance with the present invention.
  • reference numeral derstood by reference H designates a deaeration tank having concave top and bottom sections and constructed sumciently heavy to withstand a high vacuum.
  • a conduit 13 is connected to the top of the tank H.
  • the conduit l3 is provided with a pressure gauge I4 and a throttling valve 15 and a vacuum pump l'l whereby to impart a vacuum to the tank.
  • a manifold 19 is positioned about the upper periphery of the tank.
  • 'A header conduit 21 is connected to the manifold at opposite sides of the tank.
  • a plu rality of connecting conduits 25 are connected between the manifold l9 and the tank H.
  • the connecting conduits 25' pass through the cylindrical wall of the tank ll into the distributor 21 which is described in greater detailbelow.
  • the distributor 21 is. positioned a. sufllcient distance below the top of the tank II to prevent spattered particles of viscose, due to the boiling of thelatter, from contacting the top of the tank.
  • the distributor directs the viscose downwardly into contact with the side wall 33 of the tank.
  • the tank is preferably rovided with an annular ring 35 which will func ion to redistribute the flow of the viscose to avoid the formation of rivulets.
  • the viscose is designated by line 31. maintained substantially level in the tank II This level is preferably constant.
  • the conduit 39 is provided with valve 40 and pump 4
  • the bypass conduit 41 functions to pass viscosefrom the outlet line back into the tank H to avoid building up 'coagulated viscose in the conduits leading to the gauge 45.
  • a temperaturebulb 49 is positioned in the manifold an accurate temperais positioned against the internalperiphery of the tank at a distance slightly above the level 1 the viscose 31.
  • the deaerated viscose is withdrawn overlapping relationship to. lip 6
  • a flow shield 69 is positioned between the bottom of lip BI and the internal periphery of the tank II. The viscose will follow flow shield 159 and will then flow along the internal periphery of the tank wall.
  • numerals II and Ila designate a tank in which the upper section is of lower section.
  • the internal periphery of.the upper section II and the internal periphery of the top of lower section Ha form the two legs of the U-shaped member of the distributing device.
  • is bent inwardly at right angles to contact the lower section lla thereby completing the U-shaped member.
  • the connecting conduits 25 are preferably provided, at the end projecting within the U-shaped member, with an opening 13 on only one side thereof. It will be readily apparent that the series of connecting conduits 25, each provided with openings on only one side of their inwardly projecting ends issuing viscose downwardly along the wall of the tank Ila.
  • the operation of the above-described device is as follows:
  • the viscose from a feed tank (not shown) is passed into conduit 23, then into header 2
  • the vacuum pump [1 has evacuated the tank II to a suflicient amount that the viscose at the temperature at which it passes into the distributor is caused to boil.
  • the pressure on the surfrom the distributor is slightly less than the vapor pressure of the viscose.
  • the viscose as it issues from between the lips 6i and G1 boils and froths with a considerable amount of spattering and at the same time ilows'downwardly along the lip Si in a continuous film.
  • the film flows down along the flow shield 89, unless the device is constructed as shown in Figure 4, and then downwardly along the internal periphery of the wall of the tank.
  • the contained air is removed together with a. very small amount of water.
  • the evaporation of the water induces a cooling of the vis-
  • the bottom of mem- - reaches the constantly maintained and the boiling point of the viscose.
  • the vacuum imparted to the tank is preferably such that the boiling point o'fth'e viscose is at a temperature of from 10 to 35 C.
  • the film of viscose flowing along the internal wall of the tank is preferably caused to fiow over an obstruction such as ring 35 whereby the film is re-formed to prevent the formation of rivulets on the wall of the tank.
  • the viscose, before it level 37, is caused to pass a temperature bulb 53 on the internal peripheryof the tank.
  • the vacuum may be manually adjusted by throttling valve l5.
  • the vacuum will be adjusted from the temperature readings of temperature gauges and 55 to maintain constant the temperature diiferential between these two readings. By 'maintaining this temperature differential constant, the amount of water removed from the viscose will remain constant and the viscose composition will be maintained uniform.
  • the viscose is constantly withdrawn through outlet conduit 39 controlled by valve and pump 4
  • the level of the viscose in the tank will be maintained substantially constant by observation of the gauge glass and control of the pump 4
  • the conduits of the gauge glass may be occasionally.
  • the deaerating apparatus is provided with automatic means for maintaining constant the temperature differential between the incoming viscose
  • the conduit l3 through which the tank II is evacuated is connected with a small tube 93 which leads to a pressure gauge 95 by means of which the vacuum in the tank may be visually determined.
  • the conduit i3 is also provided with a butterfly valve 83 by means of which the suction of the vacuum pump may be throttled.
  • the butterfly valve 83 is autmatically operated by motor diaphragm 85.
  • the motor diaphragm is in turn operated by means of the pressure contained in tube 81 leading thereto.
  • the pressure in the 53 Inasmuch as the controller per se is'no part of the present invention, the details thereof are not set forth herein.
  • the operation of the device disclosed in Figure 5 is as follows:
  • the tank II is evacuated to the point where the vacuum is sufliciently high to cause a boiling of the viscose composition which is to be deaerated.
  • the viscose is passed into the distributor and into the tank in the same manner as above described with reference to the apparatus of Figure 1.
  • the viscose froths and boils and spatters towards the center of the tank and at; the same time a film of the viscose passes downwardly into the body of the viscose contained in the lower portion of the tank.
  • the temperatures of the viscose in the manifold and in the tank adjacent'the level of the body of the viscose in the lower portion of an expansion or contraction of the hydrocarbon liquid in the bulbs 49 and 53 respectively.
  • the expanded liquid in bulb 49 is forced through capillary conduit 59 into the controller device 9
  • is provided with air under a constant pressure which pressure is used by the controller mechanism 9
  • tube 81 is determined by the temperature differential between bulbs 49 and 53 positioned respectively in the manifold l9 and on the inter nal periphery of the tank slightly above the level of the viscose.
  • The-temperature'bulb 49 is provided with a capillary tube 50 containing an expansible hydrocarbon liquid and said capillary tube is connected to'a differential temperature controller 9
  • the temperature bulb 53 is similarly provided with a capillary tube 52 which is also connected with the controller 9
  • may be any device w ch ill function to regulate an air pressure acting 0 motor diaphragm 85 in accordance with the temperature decreasing the evacuation in the tank I to maintain constant the amount of boiling of the viscose flowing. into the tank.
  • the film of viscose having the slightly increased temperature will flow into contact with bulb 53 which will compensate the controller mechanism to again maintain constant the temperature differential between the incoming viscose in the manifold and the boiling point of the viscose on the internal periphery of the tank slightly above the viscose level 31., Should the temperature of the viscose remain the same but the volume of viscose increase, there will be no immediate function of the bulb 49.
  • the pump ll used to remove the deaerated viscose continuously. from the tank H is preferably a standard constant flow gear pump.
  • Example I u A 7% cellulose, 6% caustic viscose having a salt index of e and having is pumped into the continuous deaerating tank at a rate of 245 pounds per minute. The viscose is directed downwardly against the side walls of the tank and fiows in a continuous film having a thickness of approximately inch down the side walls of the tank and into the body of viscose in the lower portion" of the tank. The body of visa temperature 'of 21 C. 1
  • a vacuum cose is maintained at a substantially constant level in the lower portion of the tank.
  • the tank is subjected initially to a vacuum corresponding to 29.2 inches of mercury, and the viscose film boils and froths as the air and a small quantity of water 25 are removed therefrom.
  • the evaporation of the water induces a cooling of the viscose andthe viscose film, as it reaches thebody of 'viscose in the lower portion of the tank, has cooled toa temperature of 18
  • the deaerated viscose is continuously pumped from the bottom of the tank at the-rate of 244 pounds per minute and sent to a supply tank for a viscose rayon spinning machine.
  • the followlng'prbcedure may be'us'ed to determine whether the dissolved air as well as the,
  • the invention is not limited to the use of any. particular evacuating device since any means of obtaining the vacuum may be used, which will produce a vacuum high enough to cause boilin of the viscose.
  • the three-stage steam jet vacuum pump is preferred, other devices such as a piston vacuum pump, a centrifugal vacuum pump, and other pump or used.
  • the tank is sufilciently large to prevent the spattering of the viscose onto any surfaces which are not continuously washed with the flowing film of viscose.
  • the top of the tank is preferably at least 18 inches above the distributor device to avoid spattered particles from contacting the top.
  • a suitably sized tank maybe one having a diameter of 6 feet anda. height of 92/ feet.
  • cylindrical tanks are preferred other shaped containers may, however, also be used; for example, a tank having on its inner surface large corrugations wherein the line of .corrugation is parallel to the axis of the tank may be used as a means of increasing the surface area over which the viscose flows without increasing the diameter of the tank.
  • multiple tanks such as one large tank with a smaller tank inside wherein a film of viscose is provided on the inside surface "of the large tank and on the outside surface of the small tank.
  • the output of the device may be varied depending mainly upon the rate at which the viscose is introduced into the tank provided suitable deaeration is obtained.
  • this film of viscose flowin! down the sides of the tank will vary with the amount of viscose fed to said tank.
  • the film should not be so thick that only part of the thickness of the film boils during its fiow inside the tank. The entire film should boil to obtain suit- & able results.
  • the viscose was brought into the deaeratio'n' tank at a tempera- C. and was removed at a temperature of 18*. C., a temperature differential of 3 C. Since the temperature drop of the viscose as it passes throughthe tank is a measure of the amount of water evaporated therefrom, the temperature drop is regulated and should not be too great. It would be possible to operate this device with a temperature differential as much as 20 C.,
  • subJectedto-ahigh 76 exceed 7 C.
  • the temperatureefat which thr viscose may be introduced into the tank..may vary from 15 C. to 40 C. or in some cases ever higher. At temperatures lower than'15" C., the viscose become; so viscous that it flows too slowli for pr'actical operation. he effect of tempera ture on ripening of'the viscose should be taker dissolved or 00- jet action devices may 1 from 0.3 to 3 pounds of e into consideration when operating at the higher temperatures. In deaerating liquids other than viscose, temperatures other than those given above may be used depending upon the properties 01 the liquid.
  • Viscose tends to form skins and to gel if left I, stagnant.
  • The-present apparatus is so designed that all wetted portions of the' tank wall are washed bya continuous flow oi and spatterlng on dryvportions is eliminated. By this means, stagnant areas in the deaeration system are eliminated thereby permitting the apparatus to operate for long periods or time without stopping for cleaning said apparatus.
  • viscose ripening is a function of both time and temperature. 'lf'he more accurately the t e element can be controlled, the higher the temperature which can be used. Since viscose undergoes some cooling as it enters the deaerator because of evaporation of water, it is possible to ripen at a considerably higher temperature than at present and control a if desired. By this means, it is possible in the preparation of the viscose to use an excess of carbon disulfide andto subsequently recover this excess from the viscose in the deaerating system.
  • a viscose deaerating apparatus compris cylindrical container, a vacuum pump conne ted to said container, a viscose maniiold,a plurality of viscose inlet means connecting said manifold to said container near the top thereof, a U-shaped annular viscose distributing trough positioned on mediately adjacent said inlet means, and a i'rustum-shaped viscose-directing member contacting and extending downwardly from the inner bottom edge of the trough to the side wall of said container whereby to direct the flow of viscoseissuing .trom said trough in the form of afilm downwardly and into contact with the uppermost exposed portion 01' the side wall below said trough.

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  • Engineering & Computer Science (AREA)
  • Textile Engineering (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Mechanical Engineering (AREA)
  • General Chemical & Material Sciences (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
US403007A 1941-07-18 1941-07-18 Apparatus for deaerating viscose compositions Expired - Lifetime US2355057A (en)

Priority Applications (4)

Application Number Priority Date Filing Date Title
US403007A US2355057A (en) 1941-07-18 1941-07-18 Apparatus for deaerating viscose compositions
GB6952/44A GB564153A (en) 1941-07-18 1942-07-16 Improvements in or relating to the deaeration of viscous liquids such as viscose
GB9909/42A GB561050A (en) 1941-07-18 1942-07-16 Improvements in or relating to the de-aeration of viscous liquids such as viscose
FR927413D FR927413A (fr) 1941-07-18 1946-05-27 Appareil pour la désaération des compositions de viscose

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Cited By (22)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2570171A (en) * 1946-01-23 1951-10-02 Kohorn Henry Von Deaeration apparatus
US2668598A (en) * 1949-11-21 1954-02-09 Ici Ltd Apparatus for removing gases from a liquid
US2684728A (en) * 1952-05-17 1954-07-27 Ind Rayon Corp Apparatus for removing air from viscose solution
US2714938A (en) * 1951-12-18 1955-08-09 Courtaulds Ltd Apparatus for the de-aeration of viscous liquids
US2773555A (en) * 1954-12-21 1956-12-11 American Viscose Corp Deaerators
US2774441A (en) * 1953-02-09 1956-12-18 American Enka Corp Process and apparatus for the degassing of viscose
US2804172A (en) * 1951-07-10 1957-08-27 Sharples Corp Soap deaeration
US2869674A (en) * 1955-05-13 1959-01-20 American Viscose Corp Liquid and gas separator
US2971603A (en) * 1957-04-30 1961-02-14 Schmitz William Richard Apparatus for treating material for making artificial fibers
US2977355A (en) * 1954-01-13 1961-03-28 Celanese Corp Alkali cellulose aging
US3007919A (en) * 1959-10-05 1961-11-07 American Viscose Corp Continuous viscose degasification
US3112190A (en) * 1959-06-26 1963-11-26 Bowser Inc Method and apparatus for decontaminating hydraulic fluids
US3149056A (en) * 1961-03-22 1964-09-15 Dow Chemical Co Devolatilizing apparatus
US3368330A (en) * 1966-01-15 1968-02-13 Earl H. Elliott Viscose degasification apparatus
US3540192A (en) * 1967-08-15 1970-11-17 Sunds Ab Apparatus for the de-aeration of solutions,preferentially solutions of viscose
US5044761A (en) * 1989-06-19 1991-09-03 Fuji Photo Film Co., Ltd. Dissolving and deaerating method
EP0561012A1 (fr) * 1992-03-16 1993-09-22 Asea Brown Boveri Ag Procédé et dispositif pour le traitement d'eau dans un condensateur à surface
US5509954A (en) * 1994-03-28 1996-04-23 Nordson Corporation Method and apparatus for degassing high viscosity fluids
US6482254B1 (en) * 2000-11-14 2002-11-19 E. I. Du Pont De Nemours And Company Deaerator insert
DE102008050494A1 (de) 2007-10-05 2009-04-09 Heinrich Frings Gmbh & Co Kg Vorrichtung zum Entgasen einer schäumenden Flüssigkeit, insbesondere von Bier
CN103726109A (zh) * 2013-12-20 2014-04-16 中辉人造丝有限公司 一种粘胶连续脱泡器
CN104128135A (zh) * 2014-08-07 2014-11-05 广西众昌树脂有限公司 预反应器

Cited By (23)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2570171A (en) * 1946-01-23 1951-10-02 Kohorn Henry Von Deaeration apparatus
US2668598A (en) * 1949-11-21 1954-02-09 Ici Ltd Apparatus for removing gases from a liquid
US2804172A (en) * 1951-07-10 1957-08-27 Sharples Corp Soap deaeration
US2714938A (en) * 1951-12-18 1955-08-09 Courtaulds Ltd Apparatus for the de-aeration of viscous liquids
US2684728A (en) * 1952-05-17 1954-07-27 Ind Rayon Corp Apparatus for removing air from viscose solution
US2774441A (en) * 1953-02-09 1956-12-18 American Enka Corp Process and apparatus for the degassing of viscose
US2977355A (en) * 1954-01-13 1961-03-28 Celanese Corp Alkali cellulose aging
US2773555A (en) * 1954-12-21 1956-12-11 American Viscose Corp Deaerators
US2869674A (en) * 1955-05-13 1959-01-20 American Viscose Corp Liquid and gas separator
US2971603A (en) * 1957-04-30 1961-02-14 Schmitz William Richard Apparatus for treating material for making artificial fibers
US3112190A (en) * 1959-06-26 1963-11-26 Bowser Inc Method and apparatus for decontaminating hydraulic fluids
US3007919A (en) * 1959-10-05 1961-11-07 American Viscose Corp Continuous viscose degasification
US3149056A (en) * 1961-03-22 1964-09-15 Dow Chemical Co Devolatilizing apparatus
US3368330A (en) * 1966-01-15 1968-02-13 Earl H. Elliott Viscose degasification apparatus
US3540192A (en) * 1967-08-15 1970-11-17 Sunds Ab Apparatus for the de-aeration of solutions,preferentially solutions of viscose
US5044761A (en) * 1989-06-19 1991-09-03 Fuji Photo Film Co., Ltd. Dissolving and deaerating method
EP0561012A1 (fr) * 1992-03-16 1993-09-22 Asea Brown Boveri Ag Procédé et dispositif pour le traitement d'eau dans un condensateur à surface
US5509954A (en) * 1994-03-28 1996-04-23 Nordson Corporation Method and apparatus for degassing high viscosity fluids
US6482254B1 (en) * 2000-11-14 2002-11-19 E. I. Du Pont De Nemours And Company Deaerator insert
DE102008050494A1 (de) 2007-10-05 2009-04-09 Heinrich Frings Gmbh & Co Kg Vorrichtung zum Entgasen einer schäumenden Flüssigkeit, insbesondere von Bier
AT505820B1 (de) * 2007-10-05 2009-07-15 Frings & Co Heinrich Vorrichtung zum entgasen einer schäumenden flüssigkeit, insbesondere von bier
CN103726109A (zh) * 2013-12-20 2014-04-16 中辉人造丝有限公司 一种粘胶连续脱泡器
CN104128135A (zh) * 2014-08-07 2014-11-05 广西众昌树脂有限公司 预反应器

Also Published As

Publication number Publication date
GB561050A (en) 1944-05-03
FR927413A (fr) 1947-10-29
GB564153A (en) 1944-09-14

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