WO2014140175A1 - Gravitational collision enhanced upgrading of heavy oils - Google Patents
Gravitational collision enhanced upgrading of heavy oils Download PDFInfo
- Publication number
- WO2014140175A1 WO2014140175A1 PCT/EP2014/054959 EP2014054959W WO2014140175A1 WO 2014140175 A1 WO2014140175 A1 WO 2014140175A1 EP 2014054959 W EP2014054959 W EP 2014054959W WO 2014140175 A1 WO2014140175 A1 WO 2014140175A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- oil
- cracker
- gas
- accordance
- temperature
- Prior art date
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
- C10G47/32—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions in the presence of hydrogen-generating compounds
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G11/14—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts
- C10G11/18—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised-bed" technique
- C10G11/182—Regeneration
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
- C10G47/24—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions with moving solid particles
- C10G47/30—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions with moving solid particles according to the "fluidised-bed" technique
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G55/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process
- C10G55/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only
- C10G55/06—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only including at least one catalytic cracking step
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G9/28—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid material
- C10G9/32—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid material according to the "fluidised-bed" technique
Definitions
- the present invention is related to a process for gravitational upgrading and hydrogenation of heavy oil, extra heavy oil, bitumen and the like by increasing its API value, reduction of its viscosity and removal of part of the sulphur and heavy metals in the oil.
- FCCU Catalytic cracker unit
- the final contact with the catalyst bed in the reactor completes the cracking mechanism.
- the vaporized cracked oil from the reactor is suitably separated from entrained catalyst particles by cyclones and routed to the recovery section of the unit. Here it is fractionated by conventional means to meet the product stream requirements.
- the spent catalyst is routed from the reactor to the regenerator after separation from the entrained oil. Air is introduced into the regenerator and the fluid bed of the catalyst. The air reacts with the carbon coating on the catalyst to form CO/CO 2 .
- the hot and essentially carbon-free catalyst completes the cycle by its return to the reactor.
- the flue gas leaving the regenerator is rich in CO.
- This stream is often routed to a specially designed steam generator where the CO is converted to CO 2 and the exothermic heat of reaction used for generating steam (the CO boiler).
- the CO boiler the exothermic heat of reaction used for generating steam.
- Feed stocks to the FCCU are primarily in the heavy vacuum gas oil range. Typical boiling ranges are 340 0 ( 10%) to 525 °C (90%). This allows feedstock with final boiling point up to 900C. This gas oil is limited in end point by maximum tolerable metals, although the new zeolite catalysts have demonstrated higher metal tolerance than the older silica-alumina catalysts.
- present invention is not limited by its metal content as the process reduces the metal content in the order of 90%, forming metal sulphides.
- process does not require use of an advanced catalyst, but use fine grain minerals, such as inter alia silicon oxide and olivine as heat carrier.
- the fluid catalytic cracker is usually a licensed facility. Correlations and methodology are therefore proprietary to the licensor although certain data are divulged to clients under the licensor agreement. Such data are required by clients for proper operation of the unit, and may not be divulged to third parties without the licensor's expressed permission.
- the present invention does not suffer from any of these drawbacks which will be highlighted later.
- the temperature of the energy carrier is controlled by internal cooling in the regenerator for steam production whereby a constant flow of heat carrier can be obtained.
- the extended boiling range of the feed tends to cause an uneven cracking severity.
- the lighter molecules in the feed are instantly vaporized on contact with the hot catalyst and cracking occurs. In the case of the heavier molecules vaporization is not achieved as easily. This contributes to a higher coke deposition with a higher rate of catalyst deactivation.
- the whole feed should be instantly vaporized so that a uniform cracking mechanism can commence.
- the mix temperature (which is defined as the theoretical equilibrium temperature between the un-cracked vaporized feed and the regenerated catalyst) should be close to the feed dew point temperature. In conventional units this is about 20-30 'C above the riser outlet temperature. This can be approximated by the expression:
- Mhc heat of cracking (BTU/lb or kl/kg)
- This mix temperature is also slightly dependent on the catalyst temperature.
- the present invention will show how this is solved and demonstrate that it is not needed to use two-stage regeneration.
- the spent catalyst from the reactor is delivered to the first regenerator.
- the catalyst undergoes a mild oxidation with a limited amount of air. Temperatures in this regenerator remain fairly low, around 700-750 °C.
- the catalyst is pneumatically conveyed to a second one. Here excess air is used to complete the carbon burn-off and temperatures up to 900 °C are experienced.
- the regenerated catalyst leaves this second regenerator to return to the reactor via the riser.
- the technology that applies to the two-stage regeneration process is innovative in that it achieves the burning off of the high coke without impairing the catalyst activity. In the first stage the conditions encourage the combustion of most of the hydrogen associated with the coke. A significant amount of the carbon is also burned off under mild conditions. These conditions inhibit catalyst deactivation.
- the present invention operates with a temperature of 800-900 C in the lower part of the regenerator and at 450-550C in the upper part of the regenerator, which is below the temperature presented above.
- a unique dense phase energy carrier cooling system provides a technique through which the best temperature and heat balance relationship can be maintained.
- preheating of the oil still allows a high flow of energy carrier and oil feed as the generated CO/C02 and steam from the atomization of the oil, dramatically reduces the partial pressure of the oil whereby the oil behaves as being evaporated under high vacuum.
- the gravitational accelerated colliding jets of energy carriers induces mechanical shear forces which improves the cracking, i.e. allows more of the energy to be utilized in conversion.
- the equilibrium temperature between the oil feed and the regenerated catalyst must be reached in the shortest possible time. This is required in order to ensure the rapid and homogeneous vaporization of the feed. To ensure this it is necessary to design and install a proper feed injection system. This system should ensure that any catalyst back-mixing is eliminated and that all the vaporized feed components arc subject to the same cracking severity.
- the low velocity of the energy carrier in the regenerator is accelerated by gravitational forces and reduced cross section area in two collision pipes by entrance into the oil cracker.
- MTC Mix temperature control
- This one of the novel features of the present invention namely that common mineral oxides may be used as energy carriers for oil with high metal and sulphur content. Furthermore, the use of the flue gas as heat carrier reduces the process temperature to an optimal temperature for hydrogen production by the gas/water shift.
- the off gases from the regenerator itself to carry the energy carrier, it is also possible to utilize the calorimctric heat in the gas, which reduces the energy consumption.
- the cracked products leaving the FCCU reactor represent a wide range of cuts.
- This reactor effluent is often referred to as a 'syn' -crude because of its wide range of boiling point materials.
- the 'syn'-crude assay should comprise at least a TBP (True Boiling Point) curve with an analysis of light ends, gravity versus mid-boiling point curve and a PONA for the naphtha and sulphur content versus mid-boiling point for the 'syn'-crude.
- TBP True Boiling Point
- the present invention relates to a FCCU cracking unit which aims at reducing a number of the obstacles associated with existing FCCU-units and, more specifically, shows a FCCU-unit which can be built for small scale operation at a well site whereby heavy feedstock can be processed at the source.
- feedstock with severe transport properties prumping capability
- This kind of blending is used widely in for example Venezuela and Canada.
- a basic rule is that for every barrel of oil extracted from the reservoir, 3 ⁇ 4 barrel of diluent oil is needed to blend the oil into good pumpable conditions.
- Designated Collicitor the technology makes use of the thermodynamic impact from oil droplets colliding with hot solid particles.
- the Collicitor technology is enclosed in a compact reactor/regenerator concept that inherently includes high- temperature steam generation.
- the concept relies upon high energy dissipation through the collision of 40 to 60 m/s hot solids jets at 100 to 200 kg/m capable of breaking the viscous bridges at molecular level.
- the reaction enthalpy required for thermo- mechanieal upgrading is provided from the regeneration of the solids, from which 5 residual coke is burnt off. Hydrogenation is further supported by high-temperature steam instantly impacted with the local temperature peaks caused by colliding particles, thus, enhancing desired hot spot reactions.
- the solids to be used are naturally occurring mineral particles. Olivine is used as reference material owing to its tar cracking benefits. Furthermore, the Collicitor l o process is considered complementary to common extraction techniques because it (also) provides a part of the auxiliary steam required. In current operations, steam is usually generated from natural gas, representing additional cost and environmental impacts.
- the present process comprises the following main component:
- Figure 1 is schematic flow diagram of the process according to the invention.
- Figure 2 show the re-mixing elements in the combustor and the oil cracker
- Figure 3 shows one embodiment of a cracker unit according to the invention.
- Figure 4 shows a cold experimental screening tool in plastic.
- the process is started by the combustion of oil or gas in a start up burner 3) located on a regenerator 1), heating the heat carrier i the regenerator 1).
- fuel oil and air is injected into the regenerator 1) by the air compressor 2) and fuel injector 4).
- the combustion gasses transport the heat carrier into 2 vertical collision pipes 8).
- the stream of combustion gasses and heat carrier is accelerated by gravitational forces and by reduction of the internal diameter whereby the velocity of the combustion gasses and heat carrier is increased and enters the oil cracker 9).
- the stream is diverted upwards in the oil cracker 9) and further via a transfer duct 13) to a cyclone 14).
- the heat carrier and combustion gasses are separated in the cyclone 14) where the combustion gasses are routed to a condensation unit 22) via a transfer pipe 20).
- the heat carriers fall into a down comer 15) and into a loop seal 16) having 2 exits.
- One exit line is passed on to the oil cracker 9 to port 1 1 ) and one exit line to the combustor 1) to port 6) whereby the configuration of the system transfers to a CFB (Circulating Fluidized Bed) configuration.
- CFB Cirrculating Fluidized Bed
- pre heated oil from the tank 17) is pumped to the atomization nozzle 10) where the oil is atomized by steam injected into the nozzle 10).
- the oil droplets will meet the two colliding and accelerated streams of heat carrier and combustion gasses and become energized by thermal energy from the heat carrier and combustion gasses and extreme mechanical shear forces from the colliding heat carrier and change of monientums by the change of flow direction.
- the colliding particles will give rise semi plastic impacts creating countless hotspots. The total effect of the heat carrier and combustion gasses heats, evaporates and crack the oil.
- the combustion gasses which in addition to nitrogen, consists of CO and C0 2 will react with the steam from the atomization nozzle and for hydrogen according to
- the internal o the oil cracker 9 is lined with stepwise recirculation elements which generates turbulence and cavitations in the stream which now consists of HC-gas, steam and C0 2 and NOx.
- the fuel oil injection into the regenerator 1 ) is gradual reduced whereby excess air from the compressor 2) combusts the associated coke on the heat carrier.
- the combustion temperature is in the range between 800 and 900C whereas the target temperature at the lower part of the collision pipes 8) is in the range of 400 - 600C, the excess heat in the regenerator 1 ) is reduced by cooling either with a heat exchanger 23) producing either hot water or steam or with recycling flue gas from a gas blower 21 ) or a combination of the same.
- sulphur is removed from the oil as elementary sulphur and disposed f on the heat carrier together with portion of the heavy metals in the oil.
- spent bed is discharged via a cone valve 5) and into a spent bed cooler 7) where the temperature is reduced from regenerator temperature to about 125 C .
- the spent bed is replaced by fresh heat carrier from the hopper 12).
- the produced oil is extracted from the condensation or distillation system in a conventional manner.
- Fig. 2 shows the lay-out of the re-mixing elements in both the regenerator and the oil cracker.
- the elements have a cone 24) starting at a diameter of Dl at an angle of about 30 deg. which extends at a diameter D2.
- a vertical portion 25) which ends at 26) terminates into a sharp edge where the diameter is increased to D2.
- the gaseous stream flow upwards, it is accelerated over the conical part 24) of the element and maintain its velocity over the vertical portion 25).
- the vertical portion 26 At the end of the vertical portion 26) it expands violently at the sharp edge causing extreme turbulence and reduced velocity over the portion with the increased diameter D2 causing extreme collisions between the heat carrier.
- a portion of the heat carrier can be diverted over the loop seal 16) at a reduced temperature to the oil cracker where it will blend with the stream from the collision pipes 8) thus giving the target temperature of the inflow up the oil cracker given by:
- ni g combustion gasses from regenerator, kg
- a further positive effect of the process is that the re-mixing elements reduce the risk for uncontrolled back mixing and cracking in the cyclone which is observed and controlled by the ext temperature at the inlet to the cyclone.
- the suppression of over cracking is furthermore suppressed by the fluidization stream of steam in the down comer 15) of the cyclone where the steam molecules together with the non condensable gasses dilute the oil gas flow preventing the oil molecules in re- polymerization.
- the energy consumption of the heavy oil can be expressed as:
- r p heat f evaporation of oil kJ/kg ranging from 200 - 400 kJ/kg
- C heat of cracking ranging from 500 to 2000 kJ kg
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- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
Description
Claims
Priority Applications (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
BR112015022964A BR112015022964A2 (en) | 2013-03-14 | 2014-03-13 | Improved heavy oil gravitational collision enhancement |
US14/775,899 US20160024398A1 (en) | 2013-03-14 | 2014-03-13 | Gravitational collision enhanced upgrading of heavy oils |
CA2905543A CA2905543A1 (en) | 2013-03-14 | 2014-03-13 | Gravitational collision enhanced upgrading of heavy oils |
EP14709954.3A EP2970789A1 (en) | 2013-03-14 | 2014-03-13 | Gravitational collision enhanced upgrading of heavy oils |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
MX2013002908A MX2013002908A (en) | 2013-03-14 | 2013-03-14 | Gravitational collision enhanced upgrading of heavy oils. |
MXMX/A/2013/002908 | 2013-03-14 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2014140175A1 true WO2014140175A1 (en) | 2014-09-18 |
Family
ID=50277234
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/EP2014/054959 WO2014140175A1 (en) | 2013-03-14 | 2014-03-13 | Gravitational collision enhanced upgrading of heavy oils |
Country Status (6)
Country | Link |
---|---|
US (1) | US20160024398A1 (en) |
EP (1) | EP2970789A1 (en) |
BR (1) | BR112015022964A2 (en) |
CA (1) | CA2905543A1 (en) |
MX (1) | MX2013002908A (en) |
WO (1) | WO2014140175A1 (en) |
Cited By (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN106893609A (en) * | 2015-12-21 | 2017-06-27 | 中国石油天然气集团公司 | Produce the device and method of propylene content cracked gas high and gasoline with low olefine content |
WO2021025930A1 (en) * | 2019-08-02 | 2021-02-11 | Exxonmobil Chemical Patents Inc. | Processes and systems for upgrading a hydrocarbon-containing feed |
FR3105795A1 (en) | 2019-12-30 | 2021-07-02 | Total Raffinage Chimie | INTEGRATED PROCESS FOR THERMAL CONVERSION OF A HEAVY HYDROCARBON CHARGE AND INDIRECT COMBUSTION IN A CHEMICAL OXIDE-REDUCTION LOOP |
US11352567B2 (en) | 2019-08-02 | 2022-06-07 | Exxonmobil Chemical Patents Inc. | Processes for converting organic material-containing feeds via pyrolysis |
Families Citing this family (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US11667058B2 (en) | 2018-03-25 | 2023-06-06 | Radical Plastics, Inc. | Utilization of fine mineral matter in the conversion of non-biodegradable plastic and in remediation of soils polluted with non-biodegradable plastic |
AU2021381326A1 (en) | 2020-11-18 | 2023-06-29 | Radical Plastics, Inc. | Fine mineral matter for upgrading the quality of the products of thermal or catalytic cracking or in-situ heavy oil catalytic cracking |
Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4010094A (en) * | 1974-03-14 | 1977-03-01 | Standard Oil Company | Combusting flue gas in a cracking catalyst regeneration process |
US4227990A (en) * | 1978-11-20 | 1980-10-14 | Atlantic Richfield Company | Thermal cracking of retort oil |
WO2000047695A1 (en) * | 1999-02-11 | 2000-08-17 | Industrikontakt, Ing. O. Ellingsen & Co. | Catalytic cracking process |
WO2002024835A2 (en) * | 2000-09-18 | 2002-03-28 | Ensyn Group Inc. | Products produced from rapid thermal processing of heavy hydrocarbon feedstocks |
WO2005078051A1 (en) * | 2004-02-11 | 2005-08-25 | Ellycrack As | Low temperature thermodynamic cracking and conversion for upgrading of heavy oils |
-
2013
- 2013-03-14 MX MX2013002908A patent/MX2013002908A/en unknown
-
2014
- 2014-03-13 WO PCT/EP2014/054959 patent/WO2014140175A1/en active Application Filing
- 2014-03-13 CA CA2905543A patent/CA2905543A1/en not_active Abandoned
- 2014-03-13 BR BR112015022964A patent/BR112015022964A2/en not_active Application Discontinuation
- 2014-03-13 EP EP14709954.3A patent/EP2970789A1/en not_active Withdrawn
- 2014-03-13 US US14/775,899 patent/US20160024398A1/en not_active Abandoned
Patent Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4010094A (en) * | 1974-03-14 | 1977-03-01 | Standard Oil Company | Combusting flue gas in a cracking catalyst regeneration process |
US4227990A (en) * | 1978-11-20 | 1980-10-14 | Atlantic Richfield Company | Thermal cracking of retort oil |
WO2000047695A1 (en) * | 1999-02-11 | 2000-08-17 | Industrikontakt, Ing. O. Ellingsen & Co. | Catalytic cracking process |
WO2002024835A2 (en) * | 2000-09-18 | 2002-03-28 | Ensyn Group Inc. | Products produced from rapid thermal processing of heavy hydrocarbon feedstocks |
WO2005078051A1 (en) * | 2004-02-11 | 2005-08-25 | Ellycrack As | Low temperature thermodynamic cracking and conversion for upgrading of heavy oils |
Cited By (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN106893609A (en) * | 2015-12-21 | 2017-06-27 | 中国石油天然气集团公司 | Produce the device and method of propylene content cracked gas high and gasoline with low olefine content |
WO2021025930A1 (en) * | 2019-08-02 | 2021-02-11 | Exxonmobil Chemical Patents Inc. | Processes and systems for upgrading a hydrocarbon-containing feed |
US11352567B2 (en) | 2019-08-02 | 2022-06-07 | Exxonmobil Chemical Patents Inc. | Processes for converting organic material-containing feeds via pyrolysis |
FR3105795A1 (en) | 2019-12-30 | 2021-07-02 | Total Raffinage Chimie | INTEGRATED PROCESS FOR THERMAL CONVERSION OF A HEAVY HYDROCARBON CHARGE AND INDIRECT COMBUSTION IN A CHEMICAL OXIDE-REDUCTION LOOP |
WO2021136912A1 (en) | 2019-12-30 | 2021-07-08 | Total Raffinage Chimie | Integrated method for thermal conversion and indirect combustion of a heavy hydrocarbon feedstock in a redox chemical loop for producing hydrocarbon streams and capturing the co2 produced |
Also Published As
Publication number | Publication date |
---|---|
CA2905543A1 (en) | 2014-09-18 |
MX2013002908A (en) | 2014-09-18 |
EP2970789A1 (en) | 2016-01-20 |
US20160024398A1 (en) | 2016-01-28 |
BR112015022964A2 (en) | 2017-07-18 |
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