US3271268A - Process of calcining coke - Google Patents

Process of calcining coke Download PDF

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US3271268A
US3271268A US252732A US25273263A US3271268A US 3271268 A US3271268 A US 3271268A US 252732 A US252732 A US 252732A US 25273263 A US25273263 A US 25273263A US 3271268 A US3271268 A US 3271268A
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coke
combustion zone
oxidant
combustion
temperature
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US252732A
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Victor D Allred
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Marathon Oil Co
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Marathon Oil Co
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Priority to DEO8484A priority Critical patent/DE1258386B/en
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Priority to US252732A priority patent/US3271268A/en
Priority to GB30920/63A priority patent/GB1024365A/en
Priority to DE19631471571 priority patent/DE1471571B1/en
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Assigned to MARATHON OIL COMPANY, AN OH CORP reassignment MARATHON OIL COMPANY, AN OH CORP ASSIGNS THE ENTIRE INTEREST Assignors: MARATHON PETROLEUM COMPANY
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L9/00—Treating solid fuels to improve their combustion
    • C10L9/02—Treating solid fuels to improve their combustion by chemical means
    • C10L9/06—Treating solid fuels to improve their combustion by chemical means by oxidation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J6/00—Heat treatments such as Calcining; Fusing ; Pyrolysis
    • B01J6/001—Calcining
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L9/00—Treating solid fuels to improve their combustion
    • C10L9/02—Treating solid fuels to improve their combustion by chemical means
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L9/00—Treating solid fuels to improve their combustion
    • C10L9/08—Treating solid fuels to improve their combustion by heat treatments, e.g. calcining

Definitions

  • My invention relates to calcined coke and to a process for its preparation. More particularly the invention relates to a process wherein coke is calcined by passing an oxidant and coke through a retort in a cocurrent direction.
  • the temperature rises to a peak as the combustion zone is approached and falls rapidly behind the combustion zone.
  • the temperature remains low, rises abruptly within the combustion Zone and remains high after the combustion zone is passed.
  • valve 11 here shown as a star feeder
  • Retort 12 is bell-shaped and terminates in the conical bottom portion.
  • Valve 13 discharges calcined coke from the retort without substantial loss of pressure.
  • coke After coke enters retort 12 through valve 11, it piles and moves downwardly through the retort by gravity flow.
  • the incoming coke is preheated by hot inert gas, usually flue gas, introduced through preheater gas input pipe 14 and nozzled header 15.
  • hot inert gas usually flue gas
  • preheater gas input pipe 14 and nozzled header 15 An oxidant is distributed throughout the width of the coke via oxidant input pipe 16 and header 17.
  • the unignited coke passes downwardly into the cornbustion zone 20, indicated by the dashed lines just below header 17.
  • the combustion zone tends to rise in the retort but is substantially fixed by controlling the volume of coke and oxygen-containing gas.
  • Substantially all of the available oxidant is consumed at the face of the combustion zone thereby limiting the combustion zone depth to a few inches, a small volume when compared to the total treatment zone.
  • the area below the combustion zone contains coke which is above its spontaneous ignition temperature but which, due to a lack of oxidant, does not burn. It is in this area that calcination takes place.
  • the calcination time is controlled by varying retort depth and the rate of coke and oxidant throughput. Preheating aids in temperature control and in combustible gas and liquid recovery from the furnace.
  • Combustion gases are exhausted through pipe 21, pro-- tected by flange 22, and are separated from the condensable hydrocarbons by known means such as 'by partial condensation in condenser 23. If desired, a portion of the noncondensa'ble gases can be recycled for preheating purposes into retort 12 through inlet 14. Insulation in retort 12 prevents substantial heat loss.
  • the process of this invention is useful for calcining any coked material but is particularly useful in calcining petroleum cokes.
  • the process is especially useful in calcining the so-called fluid and delayed petroleum cokes and is preferably used for this purpose. Volatile combustibles can be economically recovered where the coke contains in excess of about 15 percent by weight volatiles.
  • the oxidant used in the instant process can be oxidant gases such as fluorine, chlorine, nitrogen dioxide, and the like but is preferably oxygen or mixtures thereof with inert gases. Examples of such mixtures include air or oxygen-superheated steam mixtures.
  • the oxidant can be preheated to any desired temperature prior to use in the process.
  • the amount of oxidant required in a particular process would depend on the oxidant used, the coke to be calcined, the desired combustion zone temperature, and the desired volatile combustible matter content of the final product.
  • the amount of oxidant required can be determined for a particular process through the use of routine techniques. Generally, however, the oxidant introduced int-o a reactor will be that amount required to completely oxidize only about 225 percent, by weight, of the coke being calcined. Preferably, sufficient oxidant is utilized to completely burn from about 5 to about 10 percent, by weight of coke, of the total charge.
  • the preheating temperature, and coke and oxidant throughput should be regulated to maintain a temperature of about 540 to about 1400" C. and preferably from about 3 815 to about 1360" C. at and just below the combustion zone.
  • the highest temperatures are obtained at the forward face of the combustion zone where most of the oxygen is consumed. There is a continuing slow temperature drop as the calcined coke passes away from the com bustion front.
  • the fluidized coke had a bulk density of about 1.59 and volatile combustible (VCM) content of 5.40 percent, by weight.
  • Air was flowed into the top of the sealed tube and the exit of gases from the tube was controlled to maintain a 10-lb. pressure at the top of the tube. The pressure drop across the tube was normally about 6 lbs.
  • the yield includes only the residual
  • the combustion zone heat can be augmented.
  • noncondensable or condensable fuels in the flue gases can be recycled into the combustion zone in the preheating step.
  • the coke to be fired can be wetted with a noncoking hydrocarbon fuel prior to being passed into the furnace.
  • the particles could be Wetted with kerosene or naphtha and fed into the furnace.
  • a continuous process for calcining coke comprising in combination the steps of passing coke particles as a moving bed cocurrently into a combustion zone with an amount of oxidant stoichiometrically insufficient to cause complete combustion of the coke under conditions such that only a minor portion of the coke is oxidized, the remaining coke being calcined, without substantial oxidation, by heat imparted from the combustion; and thereafter passing both the solid and gaseous products from said combustion zone through a zone containing insufficient oxidant to support combustion.
  • the process for the preparation of the calcined petroleum coke comprising passing cocurrently into a combustion zone having a temperature of at least about 540 C. coke as a moving bed, and a stoichiometrically limited amount of oxidant insufficient to cause complete combustion of the coke, wherein combustion of the oxidant and a minor portion of coke occurs within a restricted combustion zone to form calcined coke, thereafter maintaining the coke at an elevated temperature for a predetermined period and passing both the solid and gaseous products from said combustion zone through a zone containing insufficient oxidant to support combustion and thereafter recovering calcined coke.
  • supplementary fuel is selected from the group consisting of liquid and gaseous hydrocarbon fuels.
  • oxidant is selected from the group consisting of oxygen and mixtures of oxygen with an inert gas.
  • oxidant is selected from the group consisting of the halogens, nitrogen dioxide, and oxygen-containing gases.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • General Chemical & Material Sciences (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Coke Industry (AREA)

Description

Sept. 6, 1966 INVENTOR. VICTOR D. ALLRED ATTORNEY United States My invention relates to calcined coke and to a process for its preparation. More particularly the invention relates to a process wherein coke is calcined by passing an oxidant and coke through a retort in a cocurrent direction.
Nearly everyone is acquainted with coal furnaces or with coal fires in a home grate. In both these devices the flow of air is generally countercurrent to the flow of coal or coke; and substantially all of the combustible matter is burned, the burning rate depending on the air throughput.
I have now discovered that, contrary to what would be expected, only minor amounts of coke are consumed in a furnace or retort when the air flow is reversed, i.e., the coke and oxidant flow are cocurrent and are both countercurrent to the movement of the combustion zone. Furthermore, calcined cokes of unique properties; for example, varying but generally low density, porous structure, and volatile combustible matter content; can be produced readily in simple coking furnaces. These results probably arise from the temperature profile within the retort.
In the usual furnace the temperature rises to a peak as the combustion zone is approached and falls rapidly behind the combustion zone. In the process of the instant invention, the temperature remains low, rises abruptly within the combustion Zone and remains high after the combustion zone is passed.
A study of gas flow in the two types of combustion explains this phenomenon. In the case where air flow is countercurrent to coke flow, cool air passes through the burned materials and is heated as it approaches the combustion zone. It is further heated in the combustion zone and loses its heat as it passes through the unburned matter preceding the combustion zone. In the case of cocurrent air flow, the air remains cool until it contacts the combustion zone, is rapidly heated and remains hot as it flows along with materials which have passed through the combustion zone.
I have no completely satisfactory explanation for the fact that all of the combustible matter burns in the usual situation and little burns in the process of this invention. It may be that, as the relatively cool coke contacts the combustion Zone, volatiles near the surface of the coke escape into the gas stream and burn, thereby exhausting the available oxygen so that no further burning can take place. In such a situation, the combustion would be substantially in the gas phase and would move ahead with relative rapidity leaving calcined coke rather than ash.
Conversely, in the usual process where the flow of oxidant is countercurrent to the flow of combustible matter, the volatiles are distilled off and exhausted by hot flue gases and only solids are left to burn. The combustion zone, therefore, moves more slowly through the solid phase and converts it completely to ash.
It might also be that in the usual process all of the solid combustible matter is burned because it is heated to combustion temperatures by the time it reaches the combustion zone, while in the process of this invention the combustible matter is relatively cool until it enters the combustion zone. This fact may also explain the unique properties of calcined coke made by my new process.
* atent A better understanding of my invention can be obtained 'by reference to the drawing, which is a front elevation of a retort and associated equipment suitable for the process of this invention. The retort is partly broken to show internal equipment and material movement.
Typically, sized coke is fed from hopper 10 through valve 11, here shown as a star feeder, into retort 12. The valve prevents any substantial pressure leak. Retort 12 is bell-shaped and terminates in the conical bottom portion. Valve 13 discharges calcined coke from the retort without substantial loss of pressure.
After coke enters retort 12 through valve 11, it piles and moves downwardly through the retort by gravity flow. Where desired, the incoming coke is preheated by hot inert gas, usually flue gas, introduced through preheater gas input pipe 14 and nozzled header 15. An oxidant is distributed throughout the width of the coke via oxidant input pipe 16 and header 17.
The unignited coke passes downwardly into the cornbustion zone 20, indicated by the dashed lines just below header 17. The combustion zone tends to rise in the retort but is substantially fixed by controlling the volume of coke and oxygen-containing gas.
Substantially all of the available oxidant is consumed at the face of the combustion zone thereby limiting the combustion zone depth to a few inches, a small volume when compared to the total treatment zone.
The area below the combustion zone contains coke which is above its spontaneous ignition temperature but which, due to a lack of oxidant, does not burn. It is in this area that calcination takes place. The calcination time is controlled by varying retort depth and the rate of coke and oxidant throughput. Preheating aids in temperature control and in combustible gas and liquid recovery from the furnace.
Combustion gases are exhausted through pipe 21, pro-- tected by flange 22, and are separated from the condensable hydrocarbons by known means such as 'by partial condensation in condenser 23. If desired, a portion of the noncondensa'ble gases can be recycled for preheating purposes into retort 12 through inlet 14. Insulation in retort 12 prevents substantial heat loss.
The process of this invention is useful for calcining any coked material but is particularly useful in calcining petroleum cokes. The process is especially useful in calcining the so-called fluid and delayed petroleum cokes and is preferably used for this purpose. Volatile combustibles can be economically recovered where the coke contains in excess of about 15 percent by weight volatiles.
The oxidant used in the instant process can be oxidant gases such as fluorine, chlorine, nitrogen dioxide, and the like but is preferably oxygen or mixtures thereof with inert gases. Examples of such mixtures include air or oxygen-superheated steam mixtures. The oxidant can be preheated to any desired temperature prior to use in the process.
The amount of oxidant required in a particular process would depend on the oxidant used, the coke to be calcined, the desired combustion zone temperature, and the desired volatile combustible matter content of the final product. The amount of oxidant required can be determined for a particular process through the use of routine techniques. Generally, however, the oxidant introduced int-o a reactor will be that amount required to completely oxidize only about 225 percent, by weight, of the coke being calcined. Preferably, sufficient oxidant is utilized to completely burn from about 5 to about 10 percent, by weight of coke, of the total charge.
The preheating temperature, and coke and oxidant throughput should be regulated to maintain a temperature of about 540 to about 1400" C. and preferably from about 3 815 to about 1360" C. at and just below the combustion zone. The highest temperatures are obtained at the forward face of the combustion zone where most of the oxygen is consumed. There is a continuing slow temperature drop as the calcined coke passes away from the com bustion front.
The following example further illustrates my invention; and it is not intended that my process be limited to operation in the furnace shown, disclosed coke, reaction temperatures, etc. Rather it is intended that all equivalents obvious to those skilled in the art be included within the scope of my invention as claimed.
Example In a series of experiments, fluidized coke, sized to pass through a 20-mesh screen, was used to fill an insulated tube furnace 3 in. ID. x 4 ft. long. The fluidized coke had a bulk density of about 1.59 and volatile combustible (VCM) content of 5.40 percent, by weight. Air was flowed into the top of the sealed tube and the exit of gases from the tube was controlled to maintain a 10-lb. pressure at the top of the tube. The pressure drop across the tube was normally about 6 lbs. The coke was ignited at the bottom of the tube with an electric heater. As the combustion front passed up the tube, heat was added to the system at the combustion zone area by use of external resistance coils. Normally the temperature of the resistance coils ranged between about 200 and 375 C.
The following table sets out various operating conditions and results. The yield includes only the residual As shown in the above example, the combustion zone heat can be augmented. Thus noncondensable or condensable fuels in the flue gases can be recycled into the combustion zone in the preheating step. Alternately, the coke to be fired can be wetted with a noncoking hydrocarbon fuel prior to being passed into the furnace. Thus, for example, the particles could be Wetted with kerosene or naphtha and fed into the furnace.
Now having described my invention, what I claim is:
1. A continuous process for calcining coke comprising in combination the steps of passing coke particles as a moving bed cocurrently into a combustion zone with an amount of oxidant stoichiometrically insufficient to cause complete combustion of the coke under conditions such that only a minor portion of the coke is oxidized, the remaining coke being calcined, without substantial oxidation, by heat imparted from the combustion; and thereafter passing both the solid and gaseous products from said combustion zone through a zone containing insufficient oxidant to support combustion.
2. The process of claim 1 wherein a supplementary fuel is also introduced into the combustion zone cocurrently with the coke and the oxidant and wherein the combustion zone temperature is maintained at from about 540 to about 1,400 C.
4. The process of claim 1 wherein the oxidant is sufficient to oxidize from about 2 to about 25% by weight of the coke.
5. The process of claim 1 wherein the combustion zone is restricted and the amount of oxidant is limited to that amount required to maintain a temperature of from about 540 to about 1,400 C. in the combustion zone.
6. The process of claim 5 wherein the combustion zone temperature is maintained at from about 815 to about 1,360 C.
7. The process of claim 5 wherein from about 5 to about 10% by weight of the coke passed into the combustion zone is burned.
8. The process of claim 1 wherein the coke and the oxidant are preheated prior to passing into the combustion zone and wherein the combustion zone is maintained at a temperature of from about 540 to about 1,400 C., and wherein the calcined coke is thereafter recovered downstream from the combustion zone.
9. The process of claim 8 wherein the combustion zone temperature is maintained within the range of from about 815 to about 1,360 C.
10. The process for the preparation of the calcined petroleum coke comprising passing cocurrently into a combustion zone having a temperature of at least about 540 C. coke as a moving bed, and a stoichiometrically limited amount of oxidant insufficient to cause complete combustion of the coke, wherein combustion of the oxidant and a minor portion of coke occurs within a restricted combustion zone to form calcined coke, thereafter maintaining the coke at an elevated temperature for a predetermined period and passing both the solid and gaseous products from said combustion zone through a zone containing insufficient oxidant to support combustion and thereafter recovering calcined coke.
11. The process of claim 10 wherein a supplementary fuel is also passed cocurrently into the combustion zone and is burned in the combustion zone with the oxidant to maintain a reaction zone temperature of from about 815 to 1,360 C.
12. The process of claim 11 wherein from about 2 to about 25% by weight of coke is oxidized in the combustion zone.
13. The process of claim 11 wherein from about 5 to about 10% by weight of the coke is oxidized in the combustion zone.
14. The process of claim 11 wherein the supplementary fuel is selected from the group consisting of liquid and gaseous hydrocarbon fuels.
15. The process of claim 11 wherein the oxidant is selected from the group consisting of oxygen and mixtures of oxygen with an inert gas.
16. The process of claim 11 wherein the oxidant is selected from the group consisting of the halogens, nitrogen dioxide, and oxygen-containing gases.
References Cited by the Examiner UNITED STATES PATENTS 870,271 11/1907 Bulley 202-93 2,755,234 7/1956 Reintjes 20231 2,998,354 8/1961 Brown et al. 202-31 3,141,834 7/1964 Allred 2027 FOREIGN PATENTS 468,405 7/1937 Great Britain.
MORRIS O. WOLK, Primary Examiner.
J. H. NEWSOME, Assistant Examiner.

Claims (1)

1. A CONTINOUS PROCESS FOR CALCINING COKE COMPRISING IN COMBINATION THE STEPS OF PASSING COKE PARTICLES AS A MOVING BED COCURRENTLY INTO A COMBUSTION ZONE WITH AN AMOUNT OF OXIDANT STOICHIOMETICALLY INSUFFICIENT TO CAUSE COMPLETE COMBUSTION OF THE COKE UNDER CONDITIONS SUCH THAT ONLY A MINOR PORTION OF THE COKE IS OXIDIZED THE REMAINING COKE BEING CALCINED, WITHOUT SUBSTANTIAL OXIDATION, BY HEAT IMPARTED FROM THE COMBUSTION; AND THEREAFTER PASSING BOTH THE SOLID AND GASEOUS PRODUCTS FROM
US252732A 1961-01-25 1963-01-21 Process of calcining coke Expired - Lifetime US3271268A (en)

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Application Number Priority Date Filing Date Title
DEO8484A DE1258386B (en) 1961-01-25 1962-01-17 Process for the continuous degassing of coal in a shaft furnace
US252732A US3271268A (en) 1963-01-21 1963-01-21 Process of calcining coke
GB30920/63A GB1024365A (en) 1963-01-21 1963-08-06 Continuous process of calcining coke
DE19631471571 DE1471571B1 (en) 1961-01-25 1963-08-12 Continuous process for calcining coke

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Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3524806A (en) * 1967-10-02 1970-08-18 Sinclair Research Inc Process of making large coke particles
US3607062A (en) * 1969-06-18 1971-09-21 Marathon Oil Co Process and apparatus for the fluidized calcining of coke
US3909211A (en) * 1973-08-31 1975-09-30 Kvb Engineering Inc Coal desulfurization process
US4169767A (en) * 1977-06-27 1979-10-02 Koa Oil Company, Limited Process for calcining coke
EP0018064A1 (en) * 1979-04-16 1980-10-29 Conoco Phillips Company Method and apparatus for calcining delayed petroleum coke
US4718984A (en) * 1986-07-18 1988-01-12 Conoco Inc. Apparatus for calcining coke
WO2016180683A1 (en) * 2015-05-12 2016-11-17 Outotec (Finland) Oy Process and apparatus for the production of calcined petroleum coke

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US870271A (en) * 1906-12-19 1907-11-05 George W Bulley Gas-producer.
GB468405A (en) * 1936-03-25 1937-07-05 Arthur Robert Griggs Improvements in the carbonisation of coal and the like carbonaceous material
US2755234A (en) * 1954-07-16 1956-07-17 Cabot Godfrey L Inc Process for making petroleum coke non-agglutinating
US2998354A (en) * 1960-02-04 1961-08-29 Exxon Research Engineering Co Transfer line heater in calcining fluid coke
US3141834A (en) * 1961-01-25 1964-07-21 Marathon Oil Co Process for continuous destructive distillation and carbonization of coal

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US870271A (en) * 1906-12-19 1907-11-05 George W Bulley Gas-producer.
GB468405A (en) * 1936-03-25 1937-07-05 Arthur Robert Griggs Improvements in the carbonisation of coal and the like carbonaceous material
US2755234A (en) * 1954-07-16 1956-07-17 Cabot Godfrey L Inc Process for making petroleum coke non-agglutinating
US2998354A (en) * 1960-02-04 1961-08-29 Exxon Research Engineering Co Transfer line heater in calcining fluid coke
US3141834A (en) * 1961-01-25 1964-07-21 Marathon Oil Co Process for continuous destructive distillation and carbonization of coal

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3524806A (en) * 1967-10-02 1970-08-18 Sinclair Research Inc Process of making large coke particles
US3607062A (en) * 1969-06-18 1971-09-21 Marathon Oil Co Process and apparatus for the fluidized calcining of coke
US3909211A (en) * 1973-08-31 1975-09-30 Kvb Engineering Inc Coal desulfurization process
US4169767A (en) * 1977-06-27 1979-10-02 Koa Oil Company, Limited Process for calcining coke
EP0018064A1 (en) * 1979-04-16 1980-10-29 Conoco Phillips Company Method and apparatus for calcining delayed petroleum coke
US4718984A (en) * 1986-07-18 1988-01-12 Conoco Inc. Apparatus for calcining coke
WO2016180683A1 (en) * 2015-05-12 2016-11-17 Outotec (Finland) Oy Process and apparatus for the production of calcined petroleum coke
CN107636128A (en) * 2015-05-12 2018-01-26 奥图泰(芬兰)公司 Method and apparatus for producing the petroleum coke through calcining

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Owner name: MARATHON OIL COMPANY, AN OH CORP

Free format text: ASSIGNS THE ENTIRE INTEREST IN ALL PATENTS AS OF JULY 10,1982 EXCEPT PATENT NOS. 3,783,944 AND 4,260,291. ASSIGNOR ASSIGNS A FIFTY PERCENT INTEREST IN SAID TWO PATENTS AS OF JULY 10,1982;ASSIGNOR:MARATHON PETROLEUM COMPANY;REEL/FRAME:004172/0421

Effective date: 19830420