US3448013A - Distillate cooling means for flash evaporators - Google Patents

Distillate cooling means for flash evaporators Download PDF

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Publication number
US3448013A
US3448013A US571581A US3448013DA US3448013A US 3448013 A US3448013 A US 3448013A US 571581 A US571581 A US 571581A US 3448013D A US3448013D A US 3448013DA US 3448013 A US3448013 A US 3448013A
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Prior art keywords
chamber
liquid
cooling
flash
evaporator
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Expired - Lifetime
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US571581A
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English (en)
Inventor
Robert E Bailie
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Westinghouse Electric Corp
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Westinghouse Electric Corp
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D1/00—Evaporating
    • B01D1/28—Evaporating with vapour compression
    • B01D1/2803—Special features relating to the vapour to be compressed
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D1/00—Evaporating
    • B01D1/28—Evaporating with vapour compression
    • B01D1/284—Special features relating to the compressed vapour
    • B01D1/2846—The compressed vapour is not directed to the same apparatus from which the vapour was taken off
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D1/00—Evaporating
    • B01D1/28—Evaporating with vapour compression
    • B01D1/289—Compressor features (e.g. constructions, details, cooling, lubrication, driving systems)
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/06—Flash distillation
    • B01D3/065—Multiple-effect flash distillation (more than two traps)
    • 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
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A20/00—Water conservation; Efficient water supply; Efficient water use
    • Y02A20/124—Water desalination
    • 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
    • Y10S203/00—Distillation: processes, separatory
    • Y10S203/18—Control

Definitions

  • the present disclosure describes a multistage flash evaporator in combination with a product liquid cooling means that is economical to construct, operate and maintain.
  • the disclosure further includes an effective and efficient method of cooling the product liquid.
  • the present invention employs a cooling chamber in fluid communication with the last stage of a liash evaporator, and maintained at a lower pressure value than the last stage.
  • the product liquid collected in the condenser space 3,448,013 Patented June 3, 1969 ICC of the last stage is permitted to flow into the cooling chamber where a portion of the product liquid flashes into vapor.
  • the vapor is cooled by a heat exchange means, such as a plurality of tubes containing cool feed liquid, disposed in good heat exchange relationship with the vapor.
  • the cooled vapor condenses and returns to the product stream.
  • the cooling chamber 4 comprises an extension of the last stage condenser and condenser shell which provide the necessary heat transfer Surface.
  • a cooling system of this type requires only an additional length of condenser heat exchange tubes and a shell or wall, a partition disposed between the last stage condenser and the thus formed cooling chamber and a small single stage air ejector to maintain a vacuum in the cooling chamber slightly greater than that of the last evaporator stage.
  • the cost of such a cooling surface is reduced more than half that of liquid to liquid means and allows opti- -rnum liash evaporator design characteristics including an optimum (somewhat higher) temperature parameter for the last stage.
  • An object of the present invention is therefore, to provide an effective and eiiicient means and method for cooling a product liquid produced in a flash evaporator to a temperature substantially lower than that of the evaporator.
  • Another object of the invention is to provide for optimum ash evaporator design including an optimum temperature parameter for the Hash evaporator while simultaneously providing additional product liquid cooling at reduced cost.
  • FIGURE 1 is a diagrammatic View of a multistage flash evaporator incorporating an embodiment of the invention
  • FIG. 2 shows an alternative embodiment of the invention
  • FIG. 3 shows a preferred embodiment of the invention.
  • FIG. 1 a multistage flash evaporation system of the recirculation and regenerative heat exchange type generally designated by numeral 10.
  • the system employs a plurality of staged flash evaporation chambers generally designated by capital letters A, B and C, the number of chambers given by way of example only.
  • Chamber A is the first and highest pressure stage with the remaining lettered chambers forming evaporation stages decreasing in pressure in order of their alphabetical designation so that last stage C is the lowest pressure (highest vacuum) in system 1G.
  • the flash evaporation chambers A, B and C may be formed yby metal housing structure that is of a generally parallelopiped shape comprising to top wall 12, a bottom wall 13, vertical end walls 14 and 15, as well as front and rear walls (not shown), and vertical internal partitions 17 and 1S which cooperate with the outer wall structure to form the chambers.
  • Chambers A, B and C lare disposed in liquid communication with each other by way of interconnecting slots or orifices 21 and 22 formed in partitions 17 and 18, respectively adjacent bottom wall 13.
  • the housing structure further defines an equal plurality of condensing spaces 25, 26 and 27 for receiving the condensible vapors formed in the chambers C through A, respectively.
  • the condensing spaces are formed in the uppermost portion of the housing structure and are further defined by generally horizontally extending trays 31, 32 and 33.
  • the trays are provided with vertically extending vapor ow passages 34, 35 and 36 respectively, so that vapor formed in chambers C, B and A can ow upwardly through the flow passages in the condensing spaces 25, 26 and 27.
  • the vertical partitions 17 and 18 are further provided with apertures 38 and 39 above the trays so that the falling condensate collected in the tray 33 is free to flow through the associated aperture 39 into tray 32 to join the condensate collected therein, and finally through aperture 38 into last tray 31 to join the condensate collected therein. From tray 31, the condensate is removed, as indicated by line 41, as the produut liquid.
  • the condensing spaces 25, 26 and 27 are provided with suitable surface type heat exchangers or condensing tube structures 45, 46 and 47 (only diagrammatically shown in FIG. 1).
  • the condensing space 25 along with its associated tube structure 45 form heat rejection section generally designated C while the condensing spaces 26 and 27 along with their associated tube structures 46 and 47 form respective heat recovery sections B', A.
  • the tube structures in the heat recovery sections A' and B provide regenerative heating of the circulating liquid by the heat extracted from condensing the vapors produced in those stages.
  • a main ejector or suction device 50 is connected to the last and lowest pressure stage C by a suitable conduit 51.
  • the stages are serially connected together by way of openings 53 and 54 provided in partitions 17 and 18 respectively, so that air and other noncondensible gases can be removed frolm the stages by the ejector device 50.
  • An impure liquid such as sea or other impure water
  • a suitable (feed) pump 58 is pressurized and fed into system 10 by a suitable (feed) pump 58 and directed through the tube structure in heat reject section C' where a portion of the thus heated makeup liquid is rejected from the system as indicated by line 56.
  • the remaining and greater portion of the feed liquid is then directed through the tube structures in the heat recovery sections A and B'.
  • the pressurized, impure liquid mixes with the recirculating brine stream and is heated by the condensing vapors mentioned above.
  • the liquid is next directed to a suitable top or brine heater 60 comprising a heat exchanging tube structure 61 disposed within a suitable vessel 62 to which steam or other heated fluid is directed as indicated by arrow 63.
  • a suitable top or brine heater 60 comprising a heat exchanging tube structure 61 disposed within a suitable vessel 62 to which steam or other heated fluid is directed as indicated by arrow 63.
  • the steam if steam is used
  • the heated feed liquid is thence directed into the first ilash evaporation chamber A as indicated by Iline 65.
  • the heated liquid for evaporation is directed into the iirst and highest pressure chamber A, a portion thereof is flashed into vapor because of the reduced pressure ambient prevailing therein, and the vapor flashed therefrom is directed upwardly through ow passage 36 as indicated by dashed arrows 67 into the condensing space 27.
  • the vapor is condensed by heat transfer from the heat exchanging tube structure 47 and falls into tray 33 for collection.
  • the unilashed liquid flows through perennial 22 into the next and lower pressure stage chamber B wherein the same chain of events occur with the unashed liquid thence flowing throughrgic 21 into the lowest and last pressure Istage chamber C for nal evaporation.
  • the liquid With each event of ash evaporation, the liquid becomes more and more enriched or concentrated with its impurities which are iinally collected in the last and lowest pressure chamber stage C. From chamber C, the enriched liquid is directed through conduit 70 by a suitable pump 71. As well known in the art, a portion of the '4 enriched liquid may be removed or blown down from the system 10 via a suitable conduit such as conduit 70, as shown, so that the liquid which recirculates through the system, as indicated by line 72, may not exceed a predetermined level of enrichment or concentration.
  • a substantially pure product liquid is the result of the ash evaporation and condensing functions performed, respectively, in the flash chambers and condensing spaces.
  • the product liquid such as pure water
  • the product liquid is collected in trays 31, 32 and 33 as the rising vapors come in contact with heat exchange tube structures 45, 46 and 47, respectively, condense thereon and fall from the tubes as condensate into the trays.
  • the pure liquid (condensate) ows towards the last tray 31 through apertures 38 and 39 provided in the chamber partitions.
  • the product liquid is collected and withdrawn from the tray dividing the last evaporator stage from the last condensing space which, in the present arrangement, include chamber C and condensing space'25.
  • the temperature of the product liquid in this last stage is generally higher than that specified for consumption.
  • FIG. l An effective and eiiicient means for cooling the product liquid is therefore needed, and in accordance with the present invention there is shown such a means in FIG. l wherein a cooling chamber 75 is diagrammatically depicted and so disposed so as to receive the hotter than required product liquid as indicated by line 41.
  • Chamber 75 can comprise a simple shell or Wall structure formed by top and bottom walls 76 and 77 respectively, vertical end walls 78 and 79 as well as front and rear walls (not shown). The walls are structurally combined to form an air-tight chamber.
  • a heat exchange means such as a condensing tube structure 80, only diagrammatically shown.
  • a tray 81 for collecting condensate that forms as a result of vapors condensing on tube structure 80 in a manner to be explained hereinafter.
  • the condensate may be simply collected in the bottom of the chamber 75, in which case, the tray 81 would be unnecessary.
  • Chamber 75 is maintained at a lower pressure value than that maintained in the lowest pressure flash chamber C by virtue of an auxiliary vacuum pump or ejector means 82.
  • Ejector 82 removes air and other noncondensible gases from the chamber and as illustrated, may be arranged to exhaust them into the intake conduit 5'1 of the main ejector 50, as indicated by line 83.
  • the product liquid collected in tray 31 in the last condensing space 25 is permitted to enter tray 81 in chamber 75, where, upon entering the chamber a portion of the product liquid flashes into vapor by virtue of the reduced pressure maintained in chamber 75.
  • the ashed portion (vapor) rises into the area occupied by heat exchange tubes 80 which carry a cooling uid therethrough.
  • the cooling fluid owing through tubes 80 absorbs the heat from the product vapors with the vapors thus condensing on the tubes and falling to tray 81 as condensate.
  • the heat absorbed by the cooling fluid is carried out of chamber 75 by the fluid ow as indicated by line 84.
  • the thus cooled condensate is collected in the tray 81, thereby mixing with and cooling the unflashed portion of the product liquid which is subsequently withdrawn for use, as indicated by line 88.
  • FIG. 1 The arrangement depicted in FIG. 1 is particularly adaptable for use with existing flash evaporator systems and where it is desirable that the feed liquid be fed directly into the ash evaporator as shown. With this arrangement, no extensive and costly alteration and/or modication of existing ash evaporator systems is necessary to effect cooling of the product liquid.
  • FIG. 2 shows a modification of the arrangement of FIG. 1 in which the cooling chamber 75 again forms a unit separate from system 10 and is connected thereto.
  • like numerals refer to like parts.
  • FIG. 2 instead of using a separate parallel cooling uid for flow through the heat exchange tubes 80, the cooling iluid flows in series from the distillate cooling condenser 80 to the last reject stage condenser 45.
  • the remainder of the arrangement of FIG. 2 functions in substantially the manner described in connection with that of FIG. l. That is, chamber 75 is maintained at a lower pressure value than that maintained in lowest pressure flash chamber C by virtue of an auxiliary vacuum pump or ejector 82 which exhausts into condenser space 25 of ash chamber C as indicated by line 83a.
  • Auxiliary ejector means 82 could, if desired, exhaust into the intake conduit of main ejector 50, as shown in FIG. 1. In either case, the air and other noucondensible gases removed from charnber 75 'by the auxiliary ejector and directed to either the intake 51 or condensing space 25 are removed from the system by main ejector 50.
  • the product liquid from system is cooled in chamber 75 by the cool liquid in tubes 80 absorbing heat from the vapor that is formed when the product liquid enters tray 81 and a portion thereof flashes as a result of the reduced pressure in the chamber.
  • the heat is removed frorn chamber 75 by the ow of the cooling liquid through tubes 80 to tubes 45 in condensing space of the flash evaporator system 10.
  • FIGS. l and 2 provide a simple yet highly effective cooling means for existing flash evaporator systems and for new systems where it is desirable to have cooling chamber 75 separate from the ash evaporator system.
  • FIG. 3 there is shown the preferred embodiment of the invention in which Hash evaporator system '10 is divided physically into two separate groups of ash evaporator chambers with chamber C forming one group and chambers A and B forming the other group.
  • the system is divided in this way to provide an expedient for rejecting heat from the system in a manner to be more fully explained hereinafter.
  • the cooling chamber 75 is formed as an integral part of the flash evaporator 10 by a simple and economical extension of the wall structure forming the last condenser space 25 in flash evaporator system 10. Chamber 75 is further dened by an end wall 85 and a partition 86 (disposed opposite the end wall) the latter also serving to separate the condensing space 25 from the chamber 75.
  • the heat exchange tube structure 46 and 47 is shown in FIG. 3 as a bundle of three long and substantially parallel rows of tubes extending horizontally and in an unbroken manner through the condensing spaces 26 and 27 to opposite end walls 15a and 15b with the opposite end portions of the tube bundle opening into tube header structures 90 and 91 respectively.
  • the number of tube rows (three) is only representative, the heat exchange tube bundles in ash evaporators being formed by a large number of relatively small size diameter tubes disposed in close proximity to each other.
  • the tube structure 45 in the condensing space 25 of flash chamber C and the -tube structure 80 in the cooling chamber 75 is shown in FIG. 3 as a bundle of three long tubes extending horizontally and in unbroken succession through the space 25, through the partition 86, and through the chamber 75 to opposite end walls 14a and 85 with the opposite end portions of the tube bundle opening into tube header structures 92 and 93 respectively.
  • the number of tubes is representative only.
  • the preferred embodiment of invention employs a simple and economical extension of the heat exchange tube structure 45, in the condensing space 25, into cooling chamber 75 to form the heat exchange and cooling tube structure 80 in the chamber 75.
  • Beneath heat exchange tubes 80 may be disposed tray 81 for receiving the product liquid and collecting condensate as explained in connection with FIG. l.
  • the partition 86 is further provided with an opening 87 near the lower portion thereof for admitting the product liquid collected in the tray 31 to tray 8'1.
  • chamber 75 is maintained at a lower pressure value that the last flash chamber C by an auxiliary ejector 82 which can exhaust into either the main ejector intake 51 (as shown) or into the condensing space 25 as shown in lFIG. 2.
  • the unheated feed liquid is directed to header 93 by the feed pump 58.
  • Header 93 collects and equally distributes the liquid into the plurality of tubes forming heat exchange tube bundle portion employed to cool the vapors formed in the cooling chamber 75.
  • the feed liquid is directed to heat exchange tube bundle 45, in condensing space 25, and to header 92 where the liquid is collected from the tube bundle 45 for returning a portion of the thus heated liquid to its source (such as the sea) via suitable conduit 56 for the purpose of rejecting heat from the system ⁇ 10, the header 92 providing a convenient means for connecting the heat rejecting conduit 56 and a second conduit 94 for directing the remaining and greater portion of the liquid to heat exchange tube bundle portions 46 and 47 by Way of the header 90.
  • the liquid feeds into the header 91 where it is collected for feeding into top header 60 and thence into the flash chambers for flash evaporation as explained in connection with the arrangement shown in FIG. 1.
  • the unashed portion of the liquid in the flash chamber B is conducted to the flash chamber C by way of a suitable conduit 95 shown connected between the two chambers.
  • the product liquid collected in tray 32 is conducted to tray 31 by way of a suitable conduit l96 connected between the ash chambers B and C.
  • a suitable conduit 97 is employed to connect the condensing spaces 25 and 26, so that the main ejector 50 may remove air and other noucondensible gases serially from the ash chambers in a manner similar to -that shown in the arrangement of FIGS. 1 and 2.
  • the remainder of the system shown in FIG. 3 functions in substantially the same manner as that described in reference to FIGS. l and 2.
  • the three flash chambers shown in FIG. 3 are given by way of example only.
  • the heat rejecting section, comprising chamber C in FIG. 3 may consist of two or more ash chambers depending upon the size and total number of flash evaporation chamber stages in the system.
  • the heat removing function performed in the cooling chamber 75 is highly effective in reducing the temperature of a product liquid produced in a ilash evaporator, since vapor to liquid heat transfer rates are substantially greater than say liquid to liquid rates.
  • vapor to liquid heat transfer rates are substantially greater than say liquid to liquid rates.
  • the amount of heat transfer surface is thus greatly reduced so that the cost of the surface is less than half that of liquid arrangements.
  • the cooling chamber 75 is shown disposed at one end of the housing structure forming flash evaporator 10 and in axial alignment there ⁇ with. This is the optimum arrangement since the heat exchange tubes and connecting conduits are maintained in a straight line manner for maximum ease of fluid ilow.
  • chamber 75 it 4may not always be convenient to have chamber 75 so disposed, in which case the cooling chamber could be located to one side of or in some other relationship with evaporator stage C and condenser space without departing from the spirit and scope of the invention.
  • a multistage ash evaporator having a plurality of evaporating stages maintained at progressively lower pressure values and adapted to ash evaporate a heated irnpure feed liquid at progressively lower temperatures
  • apparatus yfor cooling only the product liquid after the impure feed liquid has undergone ashing in the last and lowest pressure stage of the flash evaporator and the product liquid has issued therefrom as the nal product liquid
  • said apparatus comprising means defining a flash chamber separate from the last and lowest pressure stage for receiving only the nal product liquid
  • said heat exchange structure being effective to cool and condense said vapor to form a relatively cool product liquid which recombines with the unilashed product liquid
  • the ash evaporator of claim 1 wherein the means for maintaining the ash chamber at the lower pressure includes a main and an auxiliary ejector means,
  • main and auxiliary ejector means having intake and outlet portions
  • the flash evaporater of claim 1 wherein the means for maintaining the separate ash chamber at the lower pressure includes a main and an auxiliary ejector means,
  • main and auxiliary ejector means having intake and outlet portions
  • the condensers include a tube structure, the tube structure associated with the lowest pressure ilash evaporating stage having a portion thereof extending into the ash chamber, means for admitting a coolant fluid into the tube structure, the tube structure portion comprising the heat exchange structure for cooling and condensing the ashed vapor of the product liquid.
  • the flash evaporator of claim 1 in which the apparatus for cooling the product liquid is a unitary structure physically separate from the plurality of ash evaporating stages and condensers, with the means for conducting the product liquid to the cooling apparatus comprising a conduit serially connected between the cooling apparatus and the condenser associated with the lowest pressure value stage.
  • the heat exchange structure comprises a tube structure for carrying a coolant fluid therethrough for cooling the ashed vapor in the ash chamber.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
  • Heat Treatment Of Water, Waste Water Or Sewage (AREA)
  • Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
US571581A 1966-08-10 1966-08-10 Distillate cooling means for flash evaporators Expired - Lifetime US3448013A (en)

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US57158166A 1966-08-10 1966-08-10

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US (1) US3448013A (enrdf_load_stackoverflow)
BE (1) BE702551A (enrdf_load_stackoverflow)
CH (1) CH478064A (enrdf_load_stackoverflow)
DE (1) DE1619750A1 (enrdf_load_stackoverflow)
GB (1) GB1120938A (enrdf_load_stackoverflow)
SE (1) SE340800B (enrdf_load_stackoverflow)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20070039324A1 (en) * 2003-06-09 2007-02-22 Taiji Inui Novel fuel production plant and seawater desalination system for use therein
US11097203B1 (en) 2020-03-10 2021-08-24 Bechtel Hydrocarbon Technology Solutions, Inc. Low energy ejector desalination system

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2759882A (en) * 1954-07-30 1956-08-21 Bethlehem Steel Corp Combined flash and vapor compression evaporator
US2908618A (en) * 1957-06-05 1959-10-13 Bethon Henry Edwin Flash-type distillation system
GB855550A (en) * 1957-05-27 1960-12-07 Richardsons Westgarth & Co Improvements in or relating to evaporators
US3119752A (en) * 1959-01-30 1964-01-28 Singmaster & Breyer Recovery of fresh water from sea water
GB958522A (en) * 1961-02-10 1964-05-21 Charles Sidney Gale Improvements relating to the desalination of saline water
GB965750A (en) * 1959-12-30 1964-08-06 Amf Internat Ltd Improvements in flash evaporators for distilling sea or other brackish water
US3259552A (en) * 1961-11-28 1966-07-05 Aqua Chem Inc Flash evaporator with distillate deaerator

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2759882A (en) * 1954-07-30 1956-08-21 Bethlehem Steel Corp Combined flash and vapor compression evaporator
GB855550A (en) * 1957-05-27 1960-12-07 Richardsons Westgarth & Co Improvements in or relating to evaporators
US2908618A (en) * 1957-06-05 1959-10-13 Bethon Henry Edwin Flash-type distillation system
US3119752A (en) * 1959-01-30 1964-01-28 Singmaster & Breyer Recovery of fresh water from sea water
GB965750A (en) * 1959-12-30 1964-08-06 Amf Internat Ltd Improvements in flash evaporators for distilling sea or other brackish water
GB958522A (en) * 1961-02-10 1964-05-21 Charles Sidney Gale Improvements relating to the desalination of saline water
US3259552A (en) * 1961-11-28 1966-07-05 Aqua Chem Inc Flash evaporator with distillate deaerator

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20070039324A1 (en) * 2003-06-09 2007-02-22 Taiji Inui Novel fuel production plant and seawater desalination system for use therein
US11097203B1 (en) 2020-03-10 2021-08-24 Bechtel Hydrocarbon Technology Solutions, Inc. Low energy ejector desalination system

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GB1120938A (en) 1968-07-24
SE340800B (enrdf_load_stackoverflow) 1971-12-06
CH478064A (de) 1969-09-15
BE702551A (enrdf_load_stackoverflow) 1968-01-15
DE1619750A1 (de) 1970-07-30

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