WO1995031265A1 - Procede de recuperation d'encres d'imprimerie usees - Google Patents

Procede de recuperation d'encres d'imprimerie usees Download PDF

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Publication number
WO1995031265A1
WO1995031265A1 PCT/US1994/005255 US9405255W WO9531265A1 WO 1995031265 A1 WO1995031265 A1 WO 1995031265A1 US 9405255 W US9405255 W US 9405255W WO 9531265 A1 WO9531265 A1 WO 9531265A1
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WO
WIPO (PCT)
Prior art keywords
ink
washup
hydroheater
zone
steam
Prior art date
Application number
PCT/US1994/005255
Other languages
English (en)
Inventor
Alan M. Hill
Michael D. Cain
Donald C. Cain
Original Assignee
Lawrence Paper Company
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Lawrence Paper Company filed Critical Lawrence Paper Company
Priority to PCT/US1994/005255 priority Critical patent/WO1995031265A1/fr
Priority to AU72424/94A priority patent/AU7242494A/en
Publication of WO1995031265A1 publication Critical patent/WO1995031265A1/fr

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D1/00—Evaporating
    • B01D1/14—Evaporating with heated gases or vapours or liquids in contact with the liquid
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D1/00—Evaporating
    • B01D1/16—Evaporating by spraying
    • B01D1/18—Evaporating by spraying to obtain dry solids

Definitions

  • the present invention is broadly concerned with a method for the recovery of aqueous and organic solvent- based printing ink wastes, which are generated in consid ⁇ erable volume in commercial printing operations, in order to greatly minimize the environmental problems attendant to treatment and disposal of such wastes. More particu ⁇ larly, it is concerned with such a method of ink waste recovery wherein waste ink sludge is first rendered flowable and then directed into a hydroheater simulta ⁇ neously with high pressure steam, in order to subject the ink wastes to conditions of elevated temperature, pressure and intense shear, and thus create a processed output.
  • dilute ink washup wastes may oe 'iirectly treated in a hydroheater without preliminary chemical treatments to obtain a desirable processed output. These outputs can then be dried and powdered, and the resultant product can be used in the formulation of ink for reuse.
  • the hydroheater output may be passed through a filter press to yield a pressed cake, which can subse ⁇ quently be dispersed and formulated as an ink.
  • Ink assembly cleaning typically involves spraying the inking assembly with water and/or other appropriate solvents which is thereafter collected as ink waste. Wastes of this charac ⁇ ter include relatively large volumes of water, together with pigment particles and ink carriers.
  • ink sludges may be placed in a landfill, although this option is becoming both expensive and of limited viabil ⁇ ity.
  • Another approach is to subject the sludges to pyro- lytic destruction. Although pyrolytic treatment is effective, it is a very expensive proposition, both from the standpoints of fuel consumption and shipping to the destruction site.
  • the present invention overcomes the problems outlined above, and provides a greatly improved technique for processing of ink wastes which yields essentially no objectionable byproducts for disposal, while at the same time allowing the valuable pigment fraction of the ink waste to be recovered and reused.
  • the method of the invention involves the steps of first providing a flowable stream of material, including print- ing ink wastes, and thereafter directing this stream into a confined zone while simultaneously passing a stream of steam into the zone.
  • the wastes are subjected to condi ⁇ tions of elevated temperature, pressure and intense shear in the confined zones thereby creating a processed ink waste which is passed out of the zone and preferably treating further by drying.
  • the ink wastes (from virtually any type of printing apparatus such as flexographic or lithographic presses) are obtained by first treating liquid printer washup material to separate out a substantial fraction of the solids and form a sludge.
  • This is a known procedure, and involves treatment of the originally fluid washup wastes with appropriate polymeric materials to cause the washup solids to float to the top of the liquid where they can be skimmed as a sludge.
  • the wet sludge is placed in a recep ⁇ tacle lined with filter paper and allowed to drain for a period of, e.g., twenty-four hours.
  • the result is a solid sludge containing from about 10-20% solids, and more preferably about 11-15% solids.
  • the sludge product is first rendered flowable and then subjected to superatmospheric shear processing within a confined zone.
  • the sludge is rendered flowable by subjecting it to stirring and recirculation, until it taker on the consistency of a "soupy" mixture.
  • the flow ⁇ able mixture is directed to the inlet of a hydroheater device, which also has an opposed inlet for a stream of incoming steam.
  • the hydroheater includes structure defining an annular restricted orifice, and the incoming waste ink stream is directed through this ori ⁇ fice.
  • the stream of steam is directed to intersect the ink waste stream as it passes through the restricted orifice.
  • the material within the ink waste stream is subjected to the requisite heating and shearing required for processing.
  • the ink waste should be subjected to a temperature of at least 300°F, more preferably from about 300-360°F, with the pressure conditions being at least about 60 psi in the zone, and more preferably from about 60-75 psi.
  • the output stream from the hydroheater is a smooth, homogeneous, shiny, black flowable mixture which has the appearance of thick black ink.
  • the processor can produce high quality printing ink from this processed output, simply by removing a portion of the water content, and mixing with otherwise conventional ink carriers.
  • the hydroheater output is dried to a very low moisture level approaching "bone dry", whereupon the dried residue is reduced by ballmilling or other means to a powder having an average particle size of from about 100-400 microns. This powder can then be reconstituted with normal ink carriers to produce a desirable black ink which can be used in virtually any commercial printing equipment.
  • the hydroheater output may be subjected to filter pressing to deliquify the flowable mixture and create a filter cake; the latter may then be subdivided and reconstituted with normal ink carriers to produce an ink.
  • the dilute, aqueous printer washup material contain ⁇ ing a minor amount of residual ink may be directly treated in the hydroheater, without the necessity of preliminary chemical treatment and sludge formation.
  • This signifi ⁇ cantly reduces equipment costs, and moreover simplifies the process.
  • Such printer washup have a solids content of up to about 5% by weight, and normally up to about 1% by weight, and a specific gravity in the range of 1 g/ml.
  • wastes include only the normal detergents used in printer washdown, together with residual ink and water.
  • the same hydroheater processing conditions may be employed in this embodiment as described previously, and likewise the same final residual ink recovery and reusable ink formation steps can also be followed.
  • Figure 1 is a partially schematic view illus ⁇ trating the preferred processing apparatus for ink waste sludges in accordance with the invention
  • Fig. 2 is a fragmentary view with parts broken away for clarity of the reaction section of a typical hydroheater device used in processing ink waste issedges; and
  • Fig. 3 is a schematic illustration of presently preferred in-plant apparatus for the processing and treatment of printing ink wastes.
  • a system 10 for processing of ink wastes i ⁇ illus ⁇ trated includes a sludge liquification assembly 12, steam system 14, hydroheater 16 and downstream processing assembly 18.
  • the liquification assembly 12 includes an upright, open top mixing vessel 20 presenting a frustoconical bottom 22 terminating in an outlet 24.
  • a mixer 26 is situated within vessel 20 and includes an elongated shaft 28 equipped with a pair of spaced apart, three-bladed mixing elements 30, 32, as well as an ink mixing prop 34 between the elements 30, 32.
  • the shaft 28 is coupled to an electric motor 36 for high speed rotation thereof.
  • Vessel outlet 24 is coupled to an outlet pipe 38 which leads to the input of a Moyno pump 40, the latter being driven through a motor and Reeves drive assembly 42.
  • a drain pipe 44 equipped with a ball valve 46 is connected to the pipe 38 intermediate the ends thereof as shown.
  • the output of pump 40 is connected to a recircu- lation pipe 48 which leads back to and has an open end terminating within vessel 20.
  • the pipe 48 is equipped with a ball valve 50, and a processing line 52 is teed from the recirculation pipe 48 upstream of the valve 50.
  • Processing line 52 has a control ball valve 54 therein as well as a teed drain pipe 56, controlled by ball valve 58, pressure gauge 60 and check valve 62.
  • the end of line 52 remote from recirculation 48 is coupled to the inlet of hydroheater 16.
  • Steam system 14 is conventional, and includes a boiler (not shown) coupled with a steam delivery line 64.
  • the latter has a pressure gauge 66, gate-type steam valve 68, condensate separator 70, check valve 72 and gate valve 74 therein.
  • the delivery end of line 64 is coupled to the steam inlet of hydroheater 16 as illustrated.
  • a drain line 76 equipped with trap 78 is coupled with the separa- tor 70.
  • the hydroheater 16 is illustrated in detail. Specifically, the hydroheater 16 is in the form of an elongated tubular body or combining tube 80 presenting a tubular inlet 82 for material to be processed, and an opposed, tubular steam inlet 84.
  • the hydroheater includes a frustoconical wall 86 together with an elongated, axially oriented and adjustable tubular wall 88.
  • a rotatable steam needle valve 90 extends into the body 80 and has a tapered end 92 which is complemental with frustoconical wall 86.
  • the wall 86 and end 92 cooperatively define a steam outlet orifice 94.
  • a restricted annular orifice 95 is defined between the walls 86, 88 as depicted. It will also be evident that rotation of needle valve 90 has the effect of enlarging or restricting the dimensions of the steam orifice 94.
  • tubular inlet 84 communicates with the interior of body 80 upstream of the largest diameter end of wall 86, so that incoming steam is forced to pass through orifice 94.
  • material inlet 84 is oriented such that incoming liquified sludge material is directed into body 80 downstream of wall 86, and must pass through orifice 95.
  • the hydroheater 16 is designed so that steam entering inlet 84 is caused to intersect with the stream to be processed as the latter passes through the orifice 95.
  • the processing assembly 18 includes an output delivery pipe 98 equipped with temperature and pressure gauges 100, 102 and back pressure gate valve 104.
  • the end of pipe 98 remote from hydroheater 16 communicates with a blow down chamber 106.
  • the latter has an overhead steam outlet pipe 108 extending from the upper end thereof, as well as a fin ⁇ ished product line 110 extending from its lower end and having ball control valve 112 therein.
  • drained ink waste sludge is placed within vessel 20, and mixer 26 is activated. If necessary, a small quantity of water may be added to the vessel 20 as well. High speed mixing within the vessel 20 is initiated and continues until the sludge becomes flowable.
  • valves 46, 54 and 58 are closed, and valve 50 is open.
  • valve 50 is closed and valve 54 is opened. This serves to direct the liquified sludge through line 52 for passage into hydro- heater 16 via inlet 82.
  • high pressure steam is directed through line 64 (valves 68, 74 being open) to hydroheater 16 through steam inlet 84.
  • the liquified ink sludge is heated and subjected to increased temperatures and intense shearing action. This occurs primarily at the region of intersection between the material stream received through inlet 82, and the stream of steam from inlet 84.
  • the processed output from the hydroheater 16 leaves via outlet 96 and is directed through pipe 98 to blow dowr chamber 106. In the chamber 106, excess steam is flashed off, and the final processed product is delivered through line 110 for collection.
  • the processed output from line 110 can be partially dried and a high quality ink product made directly using this material.
  • the flowable output can be completely dried and reduced to a powder which can then be reconstituted as an ink.
  • Fig. 3 is a schematic illustration of preferred in-plant apparatus 114 useful in accordance with the invention.
  • the apparatus 114 includes a prelimi ⁇ nary filtering and collecting assembly 116, a modifier addition system 118, a waste separation assembly 120, hydroheater conversion system 122 and alternate d '.mstream processing assemblies, namely, drying system 124 and filter press system 126.
  • in inlet pipe 128 which conveys the incoming ink wastes, typically including indeterminate fractions of water, detergents, pigments and polymers. The precise makeup of these wastes will vary from day to day and from machine to machine. Th incoming ink wastes are first filtered to remove large particles and extraneous matter such as paper. To this end, a pair of alternately usable filters 130, 132 are provided, each equipped with relatively large pore filter media, such as screen wire. The purpose of the filters 130, 132 is to remove the relatively large diameter contaminants from the incoming stream.
  • the assembly 116 further includes a distribution box 134 having an apertured bottom which receives the throughput from filter 130 or 132 and dis ⁇ tributes the same laterally for deposit onto underlying filter paper 136, the latter traversing arcuate, apertured tray 137 and being supplied from reel 138.
  • the filter paper 136 would typically have a pore size of approximate- ly 5 microns, although this is not critical; this filter paper serves to completely remove any remaining paper fibers from the incoming ink wastes.
  • the used filter paper is collected in bin 140.
  • the fully filtered wastes then pass through tray 137 and are collected within vessel 142 equipped with stirrer 144.
  • the vessel 142 serves as a surge tank for collection of sufficient quantities of filtered wastes to merit a production run.
  • the output of vessel 142 communi ⁇ cates with pipe 146, the latter having a Moyno pump 148 interposed therein.
  • An aeration pipe 150 also communi ⁇ cates with pipe 146 downstream of pump 148, with the pipe 150 being operatively coupled to the plant air compression system (not shown) .
  • the filtered, collected wastes pass through the pipe 146, they are aerated in order to assist in downstream flotation separation.
  • the pipe 146 ultimately communicates with a static mixer 152 , the latter being surrounded by a collec ⁇ tion tank 154.
  • the purpose of this arrangement is to complete the aeration of the wastes.
  • the tank 154 is connected via pipe 156 to a second static mixer 158, the latter also being disposed within a collection tank 160.
  • a first polymer injection line 162 communicates with pipe 156 between the mixers 152, 158.
  • a conventional mixing/holding tank 164 is connected to line 102 as shown, and is designed for the mixing and holding of low molecu ⁇ lar weight polymer.
  • a Milton-Roy metering pump 166 is interposed in line 162 for accurate delivery of the low molecular weight polymer to the aerated waste stream. Thorough mixing of the low molecular weight polymer with the waste stream is assured by means of the secondary static mixer 158.
  • the output from tank 160 passes via line 168 into and through another in-line static mixer 170.
  • a high molecular weight polymer injection pipe 172 communicates with the line 168 between tank 160 and static mixer 170.
  • the pipe 172 has a Moyno metering pump 174 therein, and is connected with a mixing/holding tank 176.
  • a pH monitor 178 is operatively connected through a conventional fitting 180 into line 168, for the purpose of con inuously monitoring the pH of the process stream. This monitor also controls the operation of upstream low molecular weight polymer metering pump 166.
  • the output of line 168 downstream of in-line mixer 170 passes into an upright flocculation tank 182.
  • the tank 182 is sized so that the polymer-supplemented ink wastes generate a large, easily separable floe before reaching the upper end of the tank.
  • Tank 182 in turn communicates with an air flotation tank 184 equipped with a distribution box 186 and with an endless rake-off belt 188 adjacent the upper end thereof.
  • the flocculated material passes into tank 184, the solids fraction rises to the top of the tank whereas clear waste water settles to the bottom. This waste water is drawn off through outlet pipe 190, whereas the floe is skimmed by rake-off belt 188.
  • the pipe 190 outputs to holding tank 192, the latter having output line 194 which delivers liquid to distributor 196.
  • the waste water from the distributor 196 is filtered through filter paper 198 (20 micron) travers ⁇ ing arcuate filter support 200.
  • the filter paper 198 is drawn from reel 202, and used filter paper is deposited in bin 204.
  • the filtered water stream is ultimately collect ⁇ ed in tank 206, and can be selectively conveyed through pip e 208 equipped with pump 210 back to the plant ink cleanup system or other suitable use.
  • the skimmed floe from tank 184 passes into collection tank 212, wherefrom it is delivered to a filter paper-lined (20 micron) dumpster 214 where the sludge is drained for a suitable period, e.g., 24 hours.
  • the drained sludge from dumpster 214 is conveyed by any suitable means to the hydroheater conversion system 122.
  • This system is essentially identical with the apparatus described in Fig. 1, and therefore like refer- ence numerals have been applied to these components for ease of understanding, and no further discussion of these components is therefore necessary.
  • the apparatus 114 provides alternate downstream processing equipment for the hydroheater-converted ink wastes, namely drying system 124 and filter press system 126.
  • a collection tank 216 adapted to receive the output from finished product line 110 as shown.
  • a recirculation line 222 is connected with output line 218 for delivery of product back to the top of tank 216, this operation being controlled by means of valve 224.
  • An electrical motor-driven mixer 226 is also provided with the collection tank 216 as shown.
  • a three-way valve 228 is operatively connected with output line 218 downstream of recirculation line 222.
  • One valve output is connected with a drying system input line 230, whereas the other valve output is connected with a filter press input line 232 having pressure gauge 233 therein.
  • the drying system 124 preferably includes an auger dryer 234 adapted to receive the output from line 230.
  • the purpose of auger dryer 234 is to pcwder the incoming liquid containing the converted ink wastes, and to this end, is designed to intermittently operate and heat the liquid, driving off moisture.
  • the auger dryer 234 creates a chunk-type, dried product, which exits the auger dryer at 236 and enters hopper 238.
  • the dried chunk product within hopper 238 can be subjected to treatment in hammermill 240, and subsequently reduction in ballmill 242.
  • appropriate amounts of water and acrylic polymer e.g., Joncryl 61LV
  • the goal of this treatment is to reduce the dried product to a flowable 7.5-8 Hegman master grind for ink production.
  • the flowable output from the ballmill 242 passes through line 244 having a pump 246 therein to ink formulation tank 248 having mixer 250 therein.
  • ink formulation tank 248 having mixer 250 therein.
  • various known "let-down” vehicles are added to the master grind. This forms a complete black ink which can be used in plant printing equipment.
  • the filter press system 126 includes any conven ⁇ tional filter press 252, for example an Ertel 12" diameter filter press. As those skilled in the art will appreci ⁇ ate, such a filter press is designed to accept a plurality of appropriately sized filter media sheets 254.
  • the liquid from collection tank 216 is directed to the filter press 252 under pressure from pump 220, it being under- stood that valve 224 would be appropriately manipulated to maintain a constant pressure within the press 252 suffi ⁇ cient for deliquifying operations, but not so high as to overcome the capacity of the filter press.
  • the pressed liquid fraction passes from filter press 252 by means of pipe 256, and this continues until all clear water has been exhausted and water flow stops; this indicates that the filter media 254 is completely full and an appropriate filter cake has formed in the filter press 252.
  • This filter cake is schematically depicted at 258 in Fig. 3.
  • the filter cake 258 is then subjected to further processing as desired in order to create a finished ink.
  • the cake 258 may be. treated in a Cowles dissolver, which serves to reduce the cake to particulate form.
  • the previously described ink carriers and let-down vehicles can be added to complete the ink formulation.
  • a modified apparatus similar to that of Fig. 1 may be employed. Such modified apparatus is described in Example 3 hereof.
  • Example 1 Flexographic ink washup wastes collected from a number of flexographic printers are collected in a 4,000 gallon tank and subjected to flocculation to permit solids removal.
  • the flocculation technique is entirely conven ⁇ tional, and involves first injecting a cationic polymer (Aquafloc #412, Dearborn Division, W. R. Grace Co., Lake Zurich, Illinois) to create a pin floe, followed by air injection and introduction of an anionic polymer (Aquafloc #407) to create a large floe which can be readily skimmed. The skimmed floe is then collected in a large dumpster lined with filter paper, and allowed to drain for approxi- mately 24 hours, until the solids level is approximately 11-13% by weight.
  • a cationic polymer Aquafloc #412, Dearborn Division, W. R. Grace Co., Lake Zurich, Illinois
  • An anionic polymer Aquafloc #407
  • the solids sludge is then loaded into the vessel 20 of liquification assembly 12.
  • a small amount of water e.g., 2-3 ounces, is placed in the vessel prior to loading with sludge. This assists in starting the sludge into the pump 40.
  • the mixer 26 and pump 40 are then turned on, and the sludge begins to circulate. Circulation continues until a substantially homogeneous, liquified mixture is created.
  • the steam systiji 18 is turned on and allowed to pass through the hydroheater 16. Water from the steam and accumulation in the steam lines is extracted through the separator 70 to produce properly clean steam.
  • the back pressure valve 104 is then slowly closed until a back pressure of 60 psi and a temperature of 310°F is established. Steam is then allowed to contin ⁇ ue blowing through the system without sludge being pumped, until the pressure and temperature stabilize. At this point, the waste sludge is diverted from assembly 12 to the hydroheater 16, and temperature and pressure levels are monitored to insure stability. The liquified waste is pumped at a rate of about 1/2 gallon per minute through the hydroheater 16. The output from the hydroheater is passed to blow down chamber 106 where excess steam is vented. The processed product passes through line 110 and is collected. If necessary, a paddle may be used in vessel 20 to insure that all sludge material passes through the system.
  • the solids level of the converted final product is not a major factor, but condensation values of the steam can greatly affect drying conditions. If the steam is dry, about 1-2% moisture is added. Excess moisture should be avoided inasmuch as this requires more energy in the drying phase. Samples of the processed product are loaded into
  • the dried chips are then broken down into smaller pieces by hand, and loaded into a laboratory ball mill having a volume of 1.2 gallons. Ceramic stones are used as the grinding media with about a 3:1 stone:waste ratio being employed. The ball mill is closed and allowed to run overnight.
  • the dry, powdered material is removed from the mill and classified through a Ro-Tap shaker sieve. This unit is run for about 30 minutes to insure complete segregation and classification of parti ⁇ cles. Particles classified from about 125-180 microns are reloaded into the ball mill with grinding medium, along with conventional ink components.
  • the ball mill is charged with a mixture comprising 15% by weight of the dried, classified waste material, 60% by weight of an aqueous acrylic polymer designed for use in pigmented inks (Joncryl 130 sold by S.C. Johnson of Racine, Wisconsin), 20% by weight water and 5% of liquid anti-abrasion poly ⁇ ethylene wax emulsion (Jonwax 26, S.C. Johnson Racine, Wisconsin) .
  • the ball mill is again allowed to run over ⁇ night.
  • Example 2 This example illustrates use of a filter press system downstream of the hydroheater.
  • Example 3 This example describes a direct treatment of printer washup material without preliminary chemical treatment and sludge formation. As indicated previously, such processing permits use of simplified equipment, such as that shown in Fig. 1, thereby eliminating many of the components shown in the Fig. 3 apparatus.
  • the liquid In order to press the converted solids from the dilute liquid, the liquid is directed (1 gal./min. flow rate) to a filter press, of the type shown at 252 in Fig. 3 and equipped with six 12" diameter pulp-paper filter pads.
  • Water discharge from pipe 256 is initially dirty but, as the filters fill up, the water turns cleaner and clearer (pH 7.8) until the water flow slows and eventually stops. At this point, the filter press is full of solids and will hold no more.
  • the press is then opened and a press cake is removed for further processing, which would typically involve use of a Cowles dissolver or ball mill such as that shown at 242 in Fig. 3, in order to produce a precursor for recycled black ink.
  • the solids content of the filter cake is typically on the order of 28-40% by weight.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Paper (AREA)
  • Treatment Of Sludge (AREA)
  • Inks, Pencil-Leads, Or Crayons (AREA)

Abstract

Procédé de récupération d'encres d'imprimerie usées, limitant les problèmes posés par la pollution tout en permettant de formuler des produits utilisables. Un écoulement de matériau comprenant les déchets d'encre est dirigé vers une entrée (82) d'un dispositif d'hydroréchauffement (16), tandis que de la vapeur est dirigée à travers l'entrée opposée (84) dudit dispositif (16). Dans ce dernier, les déchets d'encre sont soumis à des températures et à des pressions élevées, ainsi qu'à un cisaillement intense, ce qui produit une sortie homogène et coulante. Celle-ci peut être séchée et mise en poudre et la poudre peut être reconstituée en tant qu'encre noire utilisable en imprimerie. Il est possible de traiter la sortie du dispositif d'hydroréchauffement (16). Celui-ci permet de supprimer le traitement chimique préliminaire, ainsi que les boues d'encre, telles que les résidus dilués de nettoyage d'une imprimante.
PCT/US1994/005255 1994-05-11 1994-05-11 Procede de recuperation d'encres d'imprimerie usees WO1995031265A1 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
PCT/US1994/005255 WO1995031265A1 (fr) 1994-05-11 1994-05-11 Procede de recuperation d'encres d'imprimerie usees
AU72424/94A AU7242494A (en) 1994-05-11 1994-05-11 Method of recovery of printing ink wastes

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Application Number Priority Date Filing Date Title
PCT/US1994/005255 WO1995031265A1 (fr) 1994-05-11 1994-05-11 Procede de recuperation d'encres d'imprimerie usees

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
NL1005685C2 (nl) * 1997-04-01 1998-10-14 Intermonde Environment Technol Werkwijze en inrichting voor het uit water afscheiden van vaste stof.

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US74878A (en) * 1868-02-25 Improvement in cleaning cloths used by bank-note engravers
US181597A (en) * 1876-08-29 Improvement in processes of renovating waste ink
US4391638A (en) * 1982-04-22 1983-07-05 J. M. Huber Corporation Method for reclaiming ink waste
US4565638A (en) * 1983-09-22 1986-01-21 Jerry Zucker Method for purifying ink
US4738785A (en) * 1987-02-13 1988-04-19 Eastman Kodak Company Waste treatment process for printing operations employing water dispersible inks
US4874515A (en) * 1987-12-22 1989-10-17 The Ink Company Ink reclamation system

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US74878A (en) * 1868-02-25 Improvement in cleaning cloths used by bank-note engravers
US181597A (en) * 1876-08-29 Improvement in processes of renovating waste ink
US4391638A (en) * 1982-04-22 1983-07-05 J. M. Huber Corporation Method for reclaiming ink waste
US4565638A (en) * 1983-09-22 1986-01-21 Jerry Zucker Method for purifying ink
US4738785A (en) * 1987-02-13 1988-04-19 Eastman Kodak Company Waste treatment process for printing operations employing water dispersible inks
US4874515A (en) * 1987-12-22 1989-10-17 The Ink Company Ink reclamation system

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
NL1005685C2 (nl) * 1997-04-01 1998-10-14 Intermonde Environment Technol Werkwijze en inrichting voor het uit water afscheiden van vaste stof.
WO1998055194A1 (fr) * 1997-04-01 1998-12-10 Intermonde Environment Technology B.V. Procede et dispositif pour la separation de matiere solide de l'eau

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AU7242494A (en) 1995-12-05

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