US3759676A - Integrated fluid coking gasification process - Google Patents

Integrated fluid coking gasification process Download PDF

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Publication number
US3759676A
US3759676A US00108709A US3759676DA US3759676A US 3759676 A US3759676 A US 3759676A US 00108709 A US00108709 A US 00108709A US 3759676D A US3759676D A US 3759676DA US 3759676 A US3759676 A US 3759676A
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United States
Prior art keywords
coke
zone
reactor
gasifying
gas
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Expired - Lifetime
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US00108709A
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English (en)
Inventor
G Lahn
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ExxonMobil Technology and Engineering Co
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Exxon Research and Engineering Co
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B55/00—Coking mineral oils, bitumen, tar, and the like or mixtures thereof with solid carbonaceous material
    • C10B55/02—Coking mineral oils, bitumen, tar, and the like or mixtures thereof with solid carbonaceous material with solid materials
    • C10B55/04—Coking mineral oils, bitumen, tar, and the like or mixtures thereof with solid carbonaceous material with solid materials with moving solid materials
    • C10B55/08—Coking mineral oils, bitumen, tar, and the like or mixtures thereof with solid carbonaceous material with solid materials with moving solid materials in dispersed form
    • C10B55/10—Coking mineral oils, bitumen, tar, and the like or mixtures thereof with solid carbonaceous material with solid materials with moving solid materials in dispersed form according to the "fluidised bed" technique
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/48—Apparatus; Plants
    • C10J3/482—Gasifiers with stationary fluidised bed
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/48—Apparatus; Plants
    • C10J3/485—Entrained flow gasifiers
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/093—Coal
    • C10J2300/0933—Coal fines for producing water gas
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0983—Additives
    • C10J2300/0993—Inert particles, e.g. as heat exchange medium in a fluidized or moving bed, heat carriers, sand

Definitions

  • a heavy carbonaceous material such as petroleum residuum is converted to distillate and gaseous products by an integrated process consisting of coking said heavy carbonaceous material in a conventional fluid coking reactor, and gasifying the coke produced in an improved three zone gasifying reactor.
  • This invention relates to a process for producing fuel gas from coke by a novel gasifying process. More particularly the gasifying process consists of a three stage process wherein cold coke is injected into a heat transfer zone before being lifted to a gas/solids disengaging zone operated at temperatures between 900 and 1800 F., and then at least in part transferred to a gasifying zone operated at temperatures between 1600 and 2200 F.
  • this invention relates to an integrated coking-gasification process. More particularly heavy carbonaceous material such as petroleum residuum is converted to a liquid and gas petroleum distillate and coke by a conventional fluid coking reactor and the coke transferred to an improved three-stage gasifying reactor to make fuel gas.
  • a heavy hydrocarbon fraction such as vacuum residuum is fed into a fluid coking reactor to produce a liquid and gas distillate product and coke.
  • the coke is then preferably transferred to a separate burner reactor where a portion of the coke is burned to heat the remaining coke to a high enough temperature sufficient to supply the heat requirement needed in the coking reactor when the coke is recycled to the coking reactor.
  • a fluid coking process such as above has encountered several problems.
  • a by-product of this reaction is S which is released in the air as a pollutant. In light of the new federal and state air pollution laws this S0 emission is not acceptable.
  • Another object of this invention is to provide a single vessel, heater-gasifier reactor process wherein the burner bed cannot unexpectedly dump in the gasifier bed.
  • Still another object of this invention is to provide a single vessel, heater-gasifier reactor that does not need a gas distributor apparatus between the heater bed and the gasifier bed.
  • a further object of this invention is to provide a single vessel, heater-gasifier reactor process which does not need high temperature slide valves or high temperature cyclones.
  • a still further object of this invention is to provide a process for the gasification of carbonaceous materials in which the production of fuel gas is maximized by pre heating the feed to the gasifier with the exiting hot gas.
  • a process is disclosed wherein carbonaceous feed material, in particular coke, is gasified in a three zone reactor in a manner which maximizes the production of fuel gas by a novel method of feed preheating. More particularly the carbonaceous material is injected into an intermediate heat transfer zone where it is contacted and lifted upwardly by the hot gases produced in a lower gasifying zone until the now hotter carbonaceous material reaches the upper disengaging zone and deposits there while the now cooler gases escape the reactor vessel through low temperature cyclones.
  • an integrated fluid coking-gasifying process wherein the coke produced in a coking reactor is injected into a three zone reactor vessel to produce fuel gas and if desired a substa ntially desulfurized hot coke product which can be injected into the fluid coking reactor to supply the heat requirements needed in that reactor, or it can be injected directly into the lower gasifying zone of the reactor vessel to produce more fuel gas, or both. More particularly the coke produced in the coking reactor is injected into an intermediate heat transfer zone where it is contacted and lifted upward by the hot gases produced in a lower gasifying zone until the new hotter coke reaches the upper disengaging zone where the cooled gas and heated coke are separated.
  • the heated coke accumulates in the disengaging zone bed from which a portion is recycled to the coking reactor and the remainder sent to the gasifier zone where it may be converted to fuel or in part withdrawn from the reactor.
  • the cooled gases escape the reactor through low temperature cyclones.
  • a heavy hydrocarbon feed is introduced into a conventional fluid coking reactor 101 by means 102.
  • This feed could include any carbon-containing material, but for economic and availability reasons vacuum or atmospheric distillation residuum is preferred.
  • Inert particles such as silica, alumina, zirconia, magnesia, alundum or mullite, or synthetically prepared or naturally occurring material such as pumice, clay, kieselguhr, diatomaceous earth, bauxite and the like may be used to form bed 103, but preferably bed 103 comprises coke particles, and more preferably coke particles whose diameters are between 40 and 400 microns.
  • Bed 103 which is maintained in a fluidized state by a fiuidizing gas such as steam or if desired also by air or other oxygen-containing gas introduced by means 104.
  • This fluidized bed 103 is maintained at a temperature between 900 and 1100 F. by coke from the disengaging zone 113 of the three zone, heater-gasifier reactor 110 introduced to the fluidized bed 103 by transfer line 105 and if desired by the burning of the residuum with the oxygen or air from means 104.
  • the feed could be preheated in a furnace, not shown, before being injected into the fluid coking reactor 101.
  • residuum is cracked to produce light liquid and gas distillate products which are removed from the reactor by cyclone means 106.
  • a coke by-product is also produced by the reactions in bed 103 and is removed by transfer line 107 and transferred to the three zone, heater-gasifier reactor 110 by a fluidizing gas such as steam introduced into transfer line 107 by line 108.
  • a fluidizing gas such as steam introduced into transfer line 107 by line 108.
  • supplementary air or oxygen may be injected in transfer line 107 by line 109.
  • the coke is then injected into an intermediate heat transfer zone 111 at a rate of 5 to 60 tons/min., preferably between and 35 tons/min., where it is contacted by the hot gases produced from reactions in a lower gasifying zone 112.
  • the quantity and velocity of these rising hot gases must be such that the coke which enters the intermediate heat transfer zone 111 is lifted up through this zone, preferably in a draft tube means 122, so that the coke may be deposited in an upper disengaging zone 113 where it can not be dumped into the lower gasifying zone 112 because of retaining walls 121 and riser means 122 connected to reactor 110.
  • a. gas velocity above ft./sec. would be suflicient to accomplish this feat.
  • a gas velocity between and 60 ft./sec. would be preferred, and a gas velocity between 40 and 50 ft./sec. most preferred.
  • the coke deposited in the upper disengaging zone 113 by a system of baflles 114 and low temperature cyclones 115 may now be transferred by line 116 to the lower gasifying zone 112 the amount of which may be controlled by low temperature slide valve 119 or recycled back to the fluid coking reactor 101 by transfer line 117 where such transfer may be aided by steam injected into transfer line 117 by line 118.
  • the coke which is transferred b line 116 through low temperature slide valve 119 to the lower gasifying zone 112 is contacted by air or oxygen from line 123 and steam from line 124 so as to bring the temperature in zone 112 to between 1600" and 2200 F., preferably 1800 F. for maximum production of fuel gas.
  • the steam and air or oxygen also serve as fluidizing gases in order to maintain the coke in the lower gasifying zone 112 in a fluidized state so as to form a fluid bed. Maintaining zone 112 as a fluid bed results in a more even distribution of heat within the zone and prevents hot spots from developing which could destroy the wall of reactor 110.
  • the temperature is then controlled by regulating the amount of and by regulating the amount of steam introduced which results endothermically with the coke to achieve the desired balance.
  • an oxygen gas rate between 0.25 and 0.4 mole O /m01e C and a steam rate between 0.25 and 1.0 mole H O/mole C is desired for O /steam gasification.
  • an air rate between 1.5 and 3.3 moles air/mole C and steam rate between 0.16 and 0.5 mole H O/mole C is desired.
  • the 0 "rate should be between 0.3 and 0.35 mole O /mole C and the steam rate between 0.5 and 0.8 mole H O/mole C. If air is injected into zone 112 an air rate between 2.0 and 3.0 moles air/mole C and a steam rate between 0.2 and 0.3 mole H O/mole C are used.
  • the gases produced, primarily H C0, C0 and S0 within zone 112 leave the zone at about the same temperature as the zone; i.e., preferably about 1800" F. These hot gases then contact the coke from the fluid coking reactor 101. Since this coke is at a temperature of onl about 950 F. there is a transfer of heat from the hot gases (1800 F.) to the cold coke (950 F.).
  • the amount of heat transferred can be controlled by the length of time the hot gases are in contact with the relatively cold coke. This contact time in turn is controlled by the feed rate of the cold coke into intermediate heat transfer zone 111, the gas rates of both the air or oxygen and that of the steam. According to the preferred gas rates stated previously this will provide for a contact time between 0.25 and 2.0 seconds, and preferably between 05 and 1.0 second. During this period of contact the hot gases cool down to temperatures between 1200" and 1050 F., and in the preferred conditions the gases exiting from reactor have a temperature of about 1150 F. By reducing the temperature of the gases to this level allows the use of low temperature cyclones 115 rather than expensive, unreliable high temperature cyclones, to remove the gases from reactor 110.
  • the coke is being heated to a temperature between 1200 and 1050 F. Under the preferred conditions the final temperature of the coke when it is deposited into the upper disengaging zone 113 is about 1150 F. At this temperature enough coke is available for transfer to the fluid coking reactor 101, and what coke remains may be transferred by line 116 to the lower gasifying zone 112.
  • a drain pipe 120 is provided that carries excess hot coke in the lower gasifying zone 112 to line 107 where the hot coke may again be introduced into the intermediate heat exchange zone.
  • the hot coke from drain pipe 120 also provides additional heat to the coke in transfer line 107 and thereby provides further flexibility in controlling the overall process heat balance.
  • a process for producing fuel gas from coke in a three-zone, single vessel reactor which comprises:
  • step (a) introducing heated coke obtained from step ((1) into a fluidized gasifying bed maintained at temperatures between 1600 and 2200 F. and positioned in the lower zone of said reactor to contact steam and an oxygen-containing gas and thereby produce a hot fuel gas;
  • step (c) introducing relatively cold coke into said inter- 5.
  • said period of time mediate zone and contacting said relatively cold coke of step (c) is between 0.25 and 2.0 seconds. with said hot fuel gas for a period of time sufiicient 5 6.
  • said heated coke is to cool the vfuel gas to a temperature below about separated from said cooled fuel gas in said disengaging 1600 F. and to heat said relatively cold coke to a zone by gravity and cyclone means. temperature above about 1050 F., at a velocity sufli- 7.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Combustion & Propulsion (AREA)
  • Dispersion Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Materials Engineering (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Coke Industry (AREA)
US00108709A 1971-01-22 1971-01-22 Integrated fluid coking gasification process Expired - Lifetime US3759676A (en)

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US10870971A 1971-01-22 1971-01-22

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US (1) US3759676A (enrdf_load_stackoverflow)
JP (1) JPS5544792B1 (enrdf_load_stackoverflow)
CA (1) CA968290A (enrdf_load_stackoverflow)
DE (1) DE2202394A1 (enrdf_load_stackoverflow)
GB (1) GB1378023A (enrdf_load_stackoverflow)
IT (1) IT946811B (enrdf_load_stackoverflow)
NL (1) NL7200893A (enrdf_load_stackoverflow)

Cited By (21)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4203759A (en) * 1978-05-01 1980-05-20 Exxon Research & Engineering Co. Process for the preparation of a vanadium-containing metallic ash concentrate
US5106587A (en) * 1987-08-11 1992-04-21 Stone & Webster Engineering Corp. Particulate solids cracking apparatus
US20060032788A1 (en) * 1999-08-20 2006-02-16 Etter Roger G Production and use of a premium fuel grade petroleum coke
US20070261714A1 (en) * 2006-05-10 2007-11-15 He Huang In-situ continuous coke deposit removal by catalytic steam gasification
US20090145810A1 (en) * 2006-11-17 2009-06-11 Etter Roger G Addition of a Reactor Process to a Coking Process
US20090152165A1 (en) * 2006-11-17 2009-06-18 Etter Roger G System and Method for Introducing an Additive into a Coking Process to Improve Quality and Yields of Coker Products
US20090209799A1 (en) * 2006-11-17 2009-08-20 Etter Roger G System and Method of Introducing an Additive with a Unique Catalyst to a Coking Process
US20100170827A1 (en) * 2006-11-17 2010-07-08 Etter Roger G Selective Cracking and Coking of Undesirable Components in Coker Recycle and Gas Oils
US9011672B2 (en) 2006-11-17 2015-04-21 Roger G. Etter System and method of introducing an additive with a unique catalyst to a coking process
WO2015195326A1 (en) 2014-06-20 2015-12-23 Exxonmobil Research And Engineering Company Fluidized bed coking with fuel gas production
FR3044014A1 (fr) * 2015-11-20 2017-05-26 Haffner Energy Dispositif et procede de thermolyse
WO2018111543A1 (en) 2016-12-15 2018-06-21 Exxonmobil Research And Engineering Company Efficient process for converting heavy oil to gasoline
WO2019099248A1 (en) 2017-11-14 2019-05-23 Exxonmobil Research And Engineering Company Fluidized coking with increased production of liquids
US10400177B2 (en) 2017-11-14 2019-09-03 Exxonmobil Research And Engineering Company Fluidized coking with increased production of liquids
US10407631B2 (en) 2017-11-14 2019-09-10 Exxonmobil Research And Engineering Company Gasification with enriched oxygen for production of synthesis gas
WO2020041001A1 (en) 2018-08-22 2020-02-27 Exxonmobil Research And Engineering Company Waste upgrading and related systems
US10703984B2 (en) 2018-11-09 2020-07-07 Exxonmobil Research And Engineering Company Fluidized coking with oxygen-containing stripping gas
WO2021086509A1 (en) 2019-11-01 2021-05-06 Exxonmobil Chemical Patents Inc. Processes and systems for quenching pyrolysis effluents
US11014810B1 (en) 2020-01-29 2021-05-25 Exxonmobil Research And Engineering Company Carbon capture, waste upgrade, and chemicals production using improved flexicoking
WO2021150285A1 (en) 2020-01-20 2021-07-29 Exxonmobil Research And Engineering Company Ethanol production methods and systems that integrate flexicoking and fermentation
US12365828B2 (en) 2021-05-11 2025-07-22 ExxonMobil Technology and Engineering Company Polyolefin-coke composite granules as a hydraulic fracturing proppant

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE3023297C2 (de) * 1980-06-21 1988-05-05 International Minerals & Chemical Luxembourg S.A., 2010 Luxembourg Verfahren zur Herstellung eines Vorproduktes für die Erzeugung von Siliziumcarbid
JPS59103839A (ja) * 1982-11-22 1984-06-15 松下電器産業株式会社 クリスパ−用組立包装箱

Cited By (38)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4203759A (en) * 1978-05-01 1980-05-20 Exxon Research & Engineering Co. Process for the preparation of a vanadium-containing metallic ash concentrate
US5106587A (en) * 1987-08-11 1992-04-21 Stone & Webster Engineering Corp. Particulate solids cracking apparatus
US20060032788A1 (en) * 1999-08-20 2006-02-16 Etter Roger G Production and use of a premium fuel grade petroleum coke
US9475992B2 (en) 1999-08-20 2016-10-25 Roger G. Etter Production and use of a premium fuel grade petroleum coke
US7883674B2 (en) 2006-05-10 2011-02-08 United Technologies Corporation In-situ continuous coke deposit removal by catalytic steam gasification
US20070261714A1 (en) * 2006-05-10 2007-11-15 He Huang In-situ continuous coke deposit removal by catalytic steam gasification
US7513260B2 (en) 2006-05-10 2009-04-07 United Technologies Corporation In-situ continuous coke deposit removal by catalytic steam gasification
US20090152172A1 (en) * 2006-05-10 2009-06-18 United Technologies Corporation In-situ continuous coke deposit removal by catalytic steam gasification
US9011672B2 (en) 2006-11-17 2015-04-21 Roger G. Etter System and method of introducing an additive with a unique catalyst to a coking process
US8394257B2 (en) 2006-11-17 2013-03-12 Roger G. Etter Addition of a reactor process to a coking process
US20090209799A1 (en) * 2006-11-17 2009-08-20 Etter Roger G System and Method of Introducing an Additive with a Unique Catalyst to a Coking Process
US8206574B2 (en) 2006-11-17 2012-06-26 Etter Roger G Addition of a reactor process to a coking process
US8361310B2 (en) 2006-11-17 2013-01-29 Etter Roger G System and method of introducing an additive with a unique catalyst to a coking process
US8372265B2 (en) 2006-11-17 2013-02-12 Roger G. Etter Catalytic cracking of undesirable components in a coking process
US8372264B2 (en) 2006-11-17 2013-02-12 Roger G. Etter System and method for introducing an additive into a coking process to improve quality and yields of coker products
US20100170827A1 (en) * 2006-11-17 2010-07-08 Etter Roger G Selective Cracking and Coking of Undesirable Components in Coker Recycle and Gas Oils
US8888991B2 (en) 2006-11-17 2014-11-18 Roger G. Etter System and method for introducing an additive into a coking process to improve quality and yields of coker products
US8968553B2 (en) 2006-11-17 2015-03-03 Roger G. Etter Catalytic cracking of undesirable components in a coking process
US20090152165A1 (en) * 2006-11-17 2009-06-18 Etter Roger G System and Method for Introducing an Additive into a Coking Process to Improve Quality and Yields of Coker Products
US9150796B2 (en) 2006-11-17 2015-10-06 Roger G. Etter Addition of a modified vapor line reactor process to a coking process
US9187701B2 (en) 2006-11-17 2015-11-17 Roger G. Etter Reactions with undesirable components in a coking process
US20090145810A1 (en) * 2006-11-17 2009-06-11 Etter Roger G Addition of a Reactor Process to a Coking Process
WO2015195326A1 (en) 2014-06-20 2015-12-23 Exxonmobil Research And Engineering Company Fluidized bed coking with fuel gas production
FR3044014A1 (fr) * 2015-11-20 2017-05-26 Haffner Energy Dispositif et procede de thermolyse
WO2017085434A1 (fr) * 2015-11-20 2017-05-26 Haffner Energy Dispositif et procede de thermolyse
US10626338B2 (en) 2016-12-15 2020-04-21 Exxonmobil Research And Engineering Company Efficient process for converting heavy oil to gasoline
WO2018111543A1 (en) 2016-12-15 2018-06-21 Exxonmobil Research And Engineering Company Efficient process for converting heavy oil to gasoline
WO2019099248A1 (en) 2017-11-14 2019-05-23 Exxonmobil Research And Engineering Company Fluidized coking with increased production of liquids
WO2019099247A1 (en) 2017-11-14 2019-05-23 Exxonmobil Research And Engineering Company Gasification with enriched oxygen for production of synthesis gas
US10400177B2 (en) 2017-11-14 2019-09-03 Exxonmobil Research And Engineering Company Fluidized coking with increased production of liquids
US10407631B2 (en) 2017-11-14 2019-09-10 Exxonmobil Research And Engineering Company Gasification with enriched oxygen for production of synthesis gas
WO2020041001A1 (en) 2018-08-22 2020-02-27 Exxonmobil Research And Engineering Company Waste upgrading and related systems
US10703984B2 (en) 2018-11-09 2020-07-07 Exxonmobil Research And Engineering Company Fluidized coking with oxygen-containing stripping gas
WO2021086509A1 (en) 2019-11-01 2021-05-06 Exxonmobil Chemical Patents Inc. Processes and systems for quenching pyrolysis effluents
US12187967B2 (en) 2019-11-01 2025-01-07 Exxonmobil Chemical Patents Inc. Processes and systems for quenching pyrolysis effluents
WO2021150285A1 (en) 2020-01-20 2021-07-29 Exxonmobil Research And Engineering Company Ethanol production methods and systems that integrate flexicoking and fermentation
US11014810B1 (en) 2020-01-29 2021-05-25 Exxonmobil Research And Engineering Company Carbon capture, waste upgrade, and chemicals production using improved flexicoking
US12365828B2 (en) 2021-05-11 2025-07-22 ExxonMobil Technology and Engineering Company Polyolefin-coke composite granules as a hydraulic fracturing proppant

Also Published As

Publication number Publication date
GB1378023A (en) 1974-12-18
JPS5544792B1 (enrdf_load_stackoverflow) 1980-11-14
DE2202394A1 (de) 1972-08-03
IT946811B (it) 1973-05-21
CA968290A (en) 1975-05-27
NL7200893A (enrdf_load_stackoverflow) 1972-07-25

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