US3647907A - Process for quenching a gas obtained by thermal cracking of hydrocarbons - Google Patents

Process for quenching a gas obtained by thermal cracking of hydrocarbons Download PDF

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Publication number
US3647907A
US3647907A US852275A US3647907DA US3647907A US 3647907 A US3647907 A US 3647907A US 852275 A US852275 A US 852275A US 3647907D A US3647907D A US 3647907DA US 3647907 A US3647907 A US 3647907A
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quenching
temperature
heat exchanger
cracked gas
oil
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US852275A
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Takehiko Sato
Hiroyuki Sagami
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Mitsubishi Chemical Corp
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Mitsubishi Petrochemical Co Ltd
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D51/00—Auxiliary pretreatment of gases or vapours to be cleaned
    • B01D51/10—Conditioning the gas to be cleaned

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  • t is a volumetric average boiling point of the feed hydrocarbons and in which 1' r 1 I and 1 is a temperature of C.) at which 10 volume percent, 30 volume percent, 50 volume percent, 70 volume percent and 90 volume percent of feed hydrocarbons is distilled in ASTM distillation, respectively, and a is a temperature in the range of 340-420 C., and T is a temperature above 450 C. but not exceeding 600 C., said temperature -(T) being a temperature of the cracked gas at an outlet of the quenching heat exchanger, and further quenching directly the cracked gas to a temperature of 150250 C. by spraying heavier oil.
  • the present invention relates to a process for quenching a high temperature cracked gas obtained by thermal cracking of hydrocarbons efiiciently and economically.
  • the cracked gas obtained by thermal cracking of hydrocarbons has generally temperature of 700900 C. Therefore, it is required to quench the high temperature cracked gas to send the gas to a successive separating zone in which the cracked gas is separated into many useful fractions. And at the same time it is required to recover the heat energy as high pressure steam from economical standpoint.
  • the quenching has to be done very quickly for preventing the polycondensation or polymerization of ice olefin, or aromatic hydrocarbons contained in the cracked gas.
  • the quenching of the cracked gas of lighter hydrocarbons than naphtha is carried out in an indirect quenching apparatus which is connected with the cracking furnace.
  • the most troublesome drawback of the conventional quenching process in which the thermal cracked gas at 750-850 C. is quenched to a temperature below 400 C. by conventional heat exchanger, is that severe coking occurs in the surfaces of tubes of quenching heat exchanger, particularly the surfaces of tubes of the outlet portion thereof.
  • An object of the present invention is to provide a quenching process of thermal cracked gas of heavier hydrocarbons than kerosene for producing olefin hydrocarbons in high yield under stable operating conditions.
  • the object described above is achieved by a process which comprises quenching indirectly the high temperature cracked gas containing lower hydrocarbons such as ethylene and propylene which is obtained by thermal cracking of a heavier hydrocarbon oil than kerosene such as kerosene, light gas oil and heavy oil in a quenching heat exchanger at a mass velocity 50-l20 kg./m. -second, preferably 60-110 kg./m. -second, and in a period of time not more than 0.05 second, preferably not more than 0.04 second and to a temperature (T) represented by the following equation:
  • the present invention is based on our discovery that the deposition of the coke on the surfaces of the tubes of the quenching heat exchanger in a thermal cracking of heavy hydrocarbons such as kerosene, light gas oil or heavy gas oil, which is a dominant factor causing the troubles on the continuous operation, can be prevented by limiting the mass velocity of the cracked gas passing therethrough to 50-120 kg./m. -sec0nd and the cooling time therein to not more than 0.05 second and regulating a temperature of the cracked gas at the outlet of the quenching heat exchanger to a specific temperature, depending upon cracking conditions and the boiling point of the feed hydrocarbons, and the tar and coke contained in the cracked gas can be discharged out of the system without deposition by succeeding oil direct quenching.
  • heavy hydrocarbons such as kerosene, light gas oil or heavy gas oil
  • the quenching in the quenching heat exchanger has an eifect of reducing a polymerization or polycondensation reaction of the quenching oil in the succeeding oil spraying quenching apparatus.
  • the present invention it is possible to suppress the deposition of cokes on the surfaces of the tubes in the quenching heat exchanger, which are brought about by the polycondensation, polymerization and car bonization of olefin, diolefin and polycyclic aromatic compounds having high boiling points contained in the cracked gas, by adjustments of the mass velocity of the cracked gas through the quenching heat exchanger, and the resi- .4 dence time of the cracked gas in the quenching heat eX- changer to specific ranges and the temperature of the cracked gas at an outlet of the quenching heat exchanger, depending upon the nature of the starting hydrocarbon oil and the thermal cracking conditions used.
  • the high mass velocity used in the present invention has an effect of removing physically the cokes adhered to the surfaces of the tubes.
  • the temperature T of the cracked gas at an outlet of quenching heat exchanger is a temperature in the range of 450600 C. depending upon a volumetric average boiling point t of the feed hydrocarbons and is represented by the following equation:
  • FIG. 1 shows the relations of the volumetric average boiling point of the feed hydrocarbons and the temperature of the cracked gas at an outlet of quenching heat exchanger. With the ranges of the temperatures of the cracked gas at an outlet of quenching heat exchanger shown in the FIG. 1, at a given feed hydrocarbons, the value of or becomes larger as the thermal cracking condition becomes severe, and vice versa.
  • the temperature of cracked gas at an outlet of quenching heat exchanger T is approximately in the range of 460540 C. for kerosene having boiling point 230 C., and 500-575 C. for light gas oil having boiling point 210-350 C., and 520-590 C. for heavy gas oil having boiling point 230-420 C. It was heretofore impossible to operate continuously the quenching heat exchanger due to the coking on the surfaces of the tubes when the cracked gas was quenched to 300380 C. at the outlet thereof, but if the temperature of the cracked gas at the outlet of the quenching heat exchanger is adjusted according to the equation described above, the continuous operation is possible for a long period of time because of the lack of the formation of the cokes and the deposit thereof.
  • the upper limit of the temperature of the cracked gas at an outlet of the quenching heat exchanger is limited from various view points including the stop of thermal cracking reactions, the prevention of undesirable secondary reactions of the highly reactive cracked gas mixture, the improvement of heat recovery and the prevention of polymerization or condensation reaction of the quenching oil used in the succeeding quenching oil injection apparatus, and it is desirable below 600 C.
  • the lower limit depends upon the formation of cokes on the surfaces of the tubes of the quenching heat exchanger. At a temperature lower than 450 C., the heavy fraction contained in the cracked gas is condensed on the surfaces of tubes of the quenching heat exchanger and form undesirable cokes. Therefore, a temperature lower than 45 0 C. is not desirable.
  • the heat transfer area of the quenching heat exchanger used in the present invention can be calculated on the basis of the temperature of the cracked gas at an outlet of quenching heat exchanger, which is determined by the above mentioned equation.
  • it is one of effective method to make a quenching heat exchanger having a maximum heat transfer area satisfying all of the desired requirements and to vary the temperature of the cracked gas at an outlet of the quenching heat exchanger by changing the pressure and level of the coolant. It is necessary to increase a temperature of cracked gas at the outlet of the quenching heat exchanger as the feed hydrocarbon become heavier and the thermal cracking conditions become more severe.
  • the present invention can be effectively practised in the vertical type quenching heat exchanger which is composed of a cooling tube consisting of a plurality of curved tubes, and a cylindrical vessel capable of accommodating the whole of the coolant which is in contact with the outer wall of the cooling tube.
  • the high temperature cracked gas is passed from the lower portion of the cylindrical type vertical quenching heat exchanger to the upper direction thereof, and thus it is possible to adjust the temperature of the cracked gas at an outlet of the quenching heat exchanger by varying the heat transfer area of the cooling tube or the level of the coolant depending upon the properties of the feed hydrocarbon and the thermal cracking conditions.
  • FIG. 2 a process according to the present invention will be explained wherein the high temperature cracked gas is quenched according to the process of the present invention and the resulting gas is fed to a separating zone in which it is separated into useful components.
  • the steam for diluting a feed hydrocarbons is introduced from an inlet (a) to a thermal cracking furnace 1 and the feed hydrocarbons are from inlet (b) introduced to the heating furnace 1.
  • the thermal cracking heat furnace 1 is composed of a convection portion 2 and a radiation portion 3. In the convection portion 2 of the heating furnace 1, a mixture of the feed hydrocarbons and steam is preheated, and in the radiation portion 3, the hydrocarbon oil is thermally cracked.
  • the thermally cracked gas mixture from the heating furnace 1 is quenched in the quenching heat exchanger 4.
  • the line 5 which connects the heating furnace 1 with the quenching heat exchanger 4 is made of a pipe as short as possbile.
  • the cracked gas mixture is rapidly introduced to the quenching heat exchanger wherein it is possible to cool the mixture to a temperature at which the thermal cracking is stopped.
  • the thermally cracked gas mixture from the quenching heat exchanger 4 reaches the quenching oil injecting apparatus 7 through the line 6, and is cooled by the heavier oil which is injected through the line 10, and the thus cooled gas is forwarded to the separating zone 9 through the line 8.
  • the mixture is separated in to the thermally cracked gas and the heavier oil in the separating zone 9, and the cracked gas is fed through the line 11 to the distillation system (not shown in the drawing) for recovering ethylene or other resulting hydrocarbons.
  • the separated heavier oil is passed through the heat exchanger 12 via the line to recover steam, and is circulated in the quenching oil injection apparatus 7, and a portion thereof is removed out of the system via line 13.
  • the temperature of the cracked gas at an outlet of the quenching heat exchanger 4 is regulated depending upon the properties of the feed hydrocarbon and the thermal cracking conditions. That is, as the volumetric average boiling point of the feed hydrocarbon or the temperature of the thermal cracking become higher, the temperature of the cracked gas at an outlet of quenching heat exchange 4 has to be elevated.
  • the coking in the quenching heat exchanger 4 which makes the continuous operation impossible may be prevented and the tarry matter contained in the cracked gas is liquefied in the quenching oil injection apparatus 7, and discharged out of the system continuously via line 13.
  • the quenching oil injection apparatus 7 the quenching oil of 2-8 times as much as the cracked gas is injected.
  • the temperature of the quenching oil to be circulated through line 10 is maintained at an optimum temperature depending upon the properties of the feed hydrocarbons to be cracked and the cracking conditions, because the properties of the quenching oil are varied depending upon the properties of the feed hydrocarbons and the cracking condition, and the deterioration of the quenching oil and the coking at the quenching portion occur at a too high temperature of quenching oil.
  • a lower temperature of quenching oil is advantageous from a standpoint of the prevention of coking in the quenching oil injection apparatus 7 and the prevention of the deterioration of the quenching oil, it is accompanied by disadvantages in that the steam pressure which is recovered at the heat exchanger 12 becomes lower or the cost of installation for heat recovery becomes increased.
  • the temperature of the quenching oil is preferably in the range of ISO-250 C.
  • the thermal cracking was conducted at a flow rate of 3000 kg./hr., of kerosene, 1950 kg./hr. of steam, and at a temperature of 780 C. at the outlet of the thermal crackmg furnace.
  • the composition of a gas at the outlet of the furnace was as shown in Table 2.
  • the quenching heat exchanger was cooled with water having a pressure of kg./cm. g.
  • initial outlet temperature of 360 C. increased to 430 C. after a continuous operation of 15 days.
  • the pressure loss was initially 0.31 kg./cm. 1t mcreased to 0.5 kg./cm. after 15 days.
  • the yield of olefin was lowered, and it was compelled to decoke the apparatus.
  • the gas leaving the quenching heat exchanger was subjected to the spraying of the heavier oil in the quenching oil injection apparatus to quench the gas to 200 C.
  • the heavier oil used as quenching oil was a heavy fraction which was separated from the cracked gas and having the properties shown in the following Table 3.
  • the quenching oil contained 10.8 weight percent as insoluble substance in n-heptane, but no coking occurred in the process line or the portion to which the quenching oil is injected.
  • the quenching oil injection apparatus was an identical apparatus used in the Comparative Example 1.
  • COMPARATIVE EXAMPLE 2 The thermal cracking of the light gas oil having the properties as shown in Table 4 was conducted using the cracking furnace and quenching heat exchanger as used in the Comparative Example 1.
  • Aromatics 20.1 volume
  • the thermal cracking was conducted at flow rates of 3000 kg./hr. of light gas oil, 2250 kg./hr. of steam, and at a temperature of 790 C. at the outlet of the thermal cracking furnace.
  • Comparative Example 2 was repeated except that the quenching heat exchanger having heat transfer surface of 56% of that of the quenching heat exchanger of the Comparative Example 1 was used and the mass velocity of the cracked gas was 75 kg./m.
  • the temperature of the cracked gas at an outlet of the quenching heat exchanger was initially 480 C. and reached 550 C. after 20 days.
  • the pressure loss was initially 0.25 kg./cm. and reached 0.38 kg./cm. after 20 days. Thereafter, the pressure loss and the temperature of the cracked gas an outlet of the quenching heat exchanger remained nearly the same and there was no neces sity of decoking of the quenching heat exchanger after 60 days.
  • the progress of the coking can be prevented and the stable continuous operation period can be greatly extended by adjusting the mass velocity and the temperature of the cracked gas at an outlet of the quenching heat exchanger within a specific range defined in the claim.
  • t is a volumetric average boiling point of the feed hydrocarbons and 10+ 30+ so-ivo-l- 90 in which r r I 2 and 1 is a temperature C.) at which 10 volume percent, 30 volume percent, 50 volume percent, 70 volume percent and 90 volume percent of feed hydrocarbons is distilled in ASTM distillation, respectively, and a is a temperature in the range of 340420 C., and T is a temperature above 450 C. but not exceeding 600 C., said temperature (T) being a temperature of the cracked gas at an outlet of the quenching heat exchanger, and further quenching directly the cracked gas to a temperature of 150-250 C. by spraying heavier oil 10 which is the heavier component of cracked gas of which recovery temperature of ASTM distillation is in the range of 200-400 C.
  • said heavier feed hydrocarbons are selected from kerosene, light gas oil and heavy gas oil.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
US852275A 1968-09-06 1969-08-22 Process for quenching a gas obtained by thermal cracking of hydrocarbons Expired - Lifetime US3647907A (en)

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JP6419668A JPS4624681B1 (enrdf_load_stackoverflow) 1968-09-06 1968-09-06

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JP (1) JPS4624681B1 (enrdf_load_stackoverflow)
DE (1) DE1945139B2 (enrdf_load_stackoverflow)
GB (1) GB1249559A (enrdf_load_stackoverflow)
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Cited By (18)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3923921A (en) * 1971-03-01 1975-12-02 Exxon Research Engineering Co Naphtha steam-cracking quench process
US4016066A (en) * 1972-08-31 1977-04-05 Idemitsu Sekiyukagaku Kabushiki Kaisha (Idemitsu Petrochemical Co., Ltd.) Method for rapid cooling of thermally cracked gases of hydrocarbons and apparatus for carrying out the method
US4150716A (en) * 1975-02-07 1979-04-24 Chiyoda Chemical Eng. & Constr. Co. Ltd. Method of heat recovery from thermally decomposed high temperature hydrocarbon gas
US4233137A (en) * 1975-02-07 1980-11-11 Chiyoda Chemical Engineering & Construction Co., Ltd. Method of heat recovering from high temperature thermally cracked hydrocarbons
EP1204718A4 (en) * 1999-06-11 2003-09-24 Exxonmobil Res & Eng Co ATTENUATION OF FOULING WITH THERMAL CRACKING OILS
RU2215774C1 (ru) * 2002-10-01 2003-11-10 Открытое акционерное общество "Всероссийский научно-исследовательский институт органического синтеза" Способ охлаждения и подготовки продуктов пиролиза к компрессии и газоразделению
US20070007173A1 (en) * 2005-07-08 2007-01-11 Strack Robert D Method for processing hydrocarbon pyrolysis effluent
US20070007172A1 (en) * 2005-07-08 2007-01-11 Strack Robert D Method for processing hydrocarbon pyrolysis effluent
US20070007174A1 (en) * 2005-07-08 2007-01-11 Strack Robert D Method for processing hydrocarbon pyrolysis effluent
WO2007082746A1 (en) 2006-01-23 2007-07-26 Saudi Basic Industries Corporation Process for the production of ethylene from natural gas with heat integration
RU2325426C2 (ru) * 2006-02-01 2008-05-27 ООО "Компания по освоению новых технологий в топливно-энергетическом комплексе "КОНТТЭК" Способ переработки углеводородного сырья
US20080179218A1 (en) * 2007-01-26 2008-07-31 Keusenkothen Paul F Process for cracking synthetic crude oil-containing feedstock
US20090030254A1 (en) * 2007-06-26 2009-01-29 Spicer David B Process and Apparatus for Cooling Liquid Bottoms from Vapor/Liquid Separator During Steam Cracking of Hydrocarbon Feedstocks
US20090074636A1 (en) * 2005-07-08 2009-03-19 Robert David Strack Method for Processing Hydrocarbon Pyrolysis Effluent
US20090085234A1 (en) * 2007-10-02 2009-04-02 Spicer David B Method And Apparatus For Cooling Pyrolysis Effluent
US20090301935A1 (en) * 2008-06-10 2009-12-10 Spicer David B Process and Apparatus for Cooling Liquid Bottoms from Vapor-Liquid Separator by Heat Exchange with Feedstock During Steam Cracking of Hydrocarbon Feedstocks
US20100174130A1 (en) * 2009-01-05 2010-07-08 Spicer David B Process for Cracking a Heavy Hydrocarbon Feedstream
US7763162B2 (en) 2005-07-08 2010-07-27 Exxonmobil Chemical Patents Inc. Method for processing hydrocarbon pyrolysis effluent

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB1390382A (en) * 1971-03-01 1975-04-09 Exxon Research Engineering Co Steam-cracking process

Cited By (37)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3923921A (en) * 1971-03-01 1975-12-02 Exxon Research Engineering Co Naphtha steam-cracking quench process
US4016066A (en) * 1972-08-31 1977-04-05 Idemitsu Sekiyukagaku Kabushiki Kaisha (Idemitsu Petrochemical Co., Ltd.) Method for rapid cooling of thermally cracked gases of hydrocarbons and apparatus for carrying out the method
US4150716A (en) * 1975-02-07 1979-04-24 Chiyoda Chemical Eng. & Constr. Co. Ltd. Method of heat recovery from thermally decomposed high temperature hydrocarbon gas
US4233137A (en) * 1975-02-07 1980-11-11 Chiyoda Chemical Engineering & Construction Co., Ltd. Method of heat recovering from high temperature thermally cracked hydrocarbons
EP1204718A4 (en) * 1999-06-11 2003-09-24 Exxonmobil Res & Eng Co ATTENUATION OF FOULING WITH THERMAL CRACKING OILS
RU2215774C1 (ru) * 2002-10-01 2003-11-10 Открытое акционерное общество "Всероссийский научно-исследовательский институт органического синтеза" Способ охлаждения и подготовки продуктов пиролиза к компрессии и газоразделению
KR100966962B1 (ko) 2005-07-08 2010-06-30 엑손모빌 케미칼 패턴츠 인코포레이티드 탄화수소 열분해 유출물을 처리하는 방법
US7763162B2 (en) 2005-07-08 2010-07-27 Exxonmobil Chemical Patents Inc. Method for processing hydrocarbon pyrolysis effluent
US20070007174A1 (en) * 2005-07-08 2007-01-11 Strack Robert D Method for processing hydrocarbon pyrolysis effluent
WO2007008406A1 (en) 2005-07-08 2007-01-18 Exxonmobil Chemical Patents Inc. Method for processing hydrocarbon pyrolysis effluent
US8524070B2 (en) 2005-07-08 2013-09-03 Exxonmobil Chemical Patents Inc. Method for processing hydrocarbon pyrolysis effluent
US8074707B2 (en) 2005-07-08 2011-12-13 Exxonmobil Chemical Patents Inc. Method for processing hydrocarbon pyrolysis effluent
US7981374B2 (en) 2005-07-08 2011-07-19 Exxonmobil Chemical Patents Inc. Method for processing hydrocarbon pyrolysis effluent
US7972482B2 (en) 2005-07-08 2011-07-05 Exxonmobile Chemical Patents Inc. Method for processing hydrocarbon pyrolysis effluent
US20090074636A1 (en) * 2005-07-08 2009-03-19 Robert David Strack Method for Processing Hydrocarbon Pyrolysis Effluent
EP2330175A2 (en) 2005-07-08 2011-06-08 ExxonMobil Chemical Patents Inc. Apparatus for processing hydrocarbon pyrolysis effluent
US20100276126A1 (en) * 2005-07-08 2010-11-04 Robert David Strack Method for Processing Hydrocarbon Pyrolysis Effluent
US20100230235A1 (en) * 2005-07-08 2010-09-16 Robert David Strack Method For Processing Hydrocarbon Pyrolysis Effluent
US20070007173A1 (en) * 2005-07-08 2007-01-11 Strack Robert D Method for processing hydrocarbon pyrolysis effluent
US7749372B2 (en) 2005-07-08 2010-07-06 Exxonmobil Chemical Patents Inc. Method for processing hydrocarbon pyrolysis effluent
US7780843B2 (en) * 2005-07-08 2010-08-24 ExxonMobil Chemical Company Patents Inc. Method for processing hydrocarbon pyrolysis effluent
US20070007172A1 (en) * 2005-07-08 2007-01-11 Strack Robert D Method for processing hydrocarbon pyrolysis effluent
US20100234476A1 (en) * 2006-01-23 2010-09-16 Yungyi Lin Process For The Production Of Ethylene From Natural Gas With Heat Integration
WO2007082746A1 (en) 2006-01-23 2007-07-26 Saudi Basic Industries Corporation Process for the production of ethylene from natural gas with heat integration
US8080697B2 (en) * 2006-01-23 2011-12-20 Saudi Basic Industries Corporation Process for the production of ethylene from natural gas with heat integration
RU2325426C2 (ru) * 2006-02-01 2008-05-27 ООО "Компания по освоению новых технологий в топливно-энергетическом комплексе "КОНТТЭК" Способ переработки углеводородного сырья
US20080179218A1 (en) * 2007-01-26 2008-07-31 Keusenkothen Paul F Process for cracking synthetic crude oil-containing feedstock
US7563357B2 (en) 2007-01-26 2009-07-21 Exxonmobil Chemical Patents Inc. Process for cracking synthetic crude oil-containing feedstock
US20090030254A1 (en) * 2007-06-26 2009-01-29 Spicer David B Process and Apparatus for Cooling Liquid Bottoms from Vapor/Liquid Separator During Steam Cracking of Hydrocarbon Feedstocks
US8158840B2 (en) 2007-06-26 2012-04-17 Exxonmobil Chemical Patents Inc. Process and apparatus for cooling liquid bottoms from vapor/liquid separator during steam cracking of hydrocarbon feedstocks
US20110233797A1 (en) * 2007-10-02 2011-09-29 Spicer David B Method And Apparatus For Cooling Pyrolysis Effluent
US20090085234A1 (en) * 2007-10-02 2009-04-02 Spicer David B Method And Apparatus For Cooling Pyrolysis Effluent
US8074973B2 (en) 2007-10-02 2011-12-13 Exxonmobil Chemical Patents Inc. Method and apparatus for cooling pyrolysis effluent
US8177200B2 (en) 2007-10-02 2012-05-15 Exxonmobil Chemical Patents Inc. Method and apparatus for cooling pyrolysis effluent
US20090301935A1 (en) * 2008-06-10 2009-12-10 Spicer David B Process and Apparatus for Cooling Liquid Bottoms from Vapor-Liquid Separator by Heat Exchange with Feedstock During Steam Cracking of Hydrocarbon Feedstocks
US20100174130A1 (en) * 2009-01-05 2010-07-08 Spicer David B Process for Cracking a Heavy Hydrocarbon Feedstream
US8684384B2 (en) 2009-01-05 2014-04-01 Exxonmobil Chemical Patents Inc. Process for cracking a heavy hydrocarbon feedstream

Also Published As

Publication number Publication date
NL155302B (nl) 1977-12-15
NL6913589A (enrdf_load_stackoverflow) 1970-03-10
DE1945139A1 (de) 1970-03-12
GB1249559A (en) 1971-10-13
JPS4624681B1 (enrdf_load_stackoverflow) 1971-07-15
DE1945139B2 (de) 1981-01-15

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