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
  • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
  • C10G1/002—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal in combination with oil conversion- or refining processes
• • 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
  • C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
• • 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
  • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
  • C10G1/10—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal from rubber or rubber waste
• • 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
  • C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
  • C10J3/56—Apparatus; Plants
• • 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
  • C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
  • C10J3/60—Processes
  • C10J3/64—Processes with decomposition of the distillation products
  • C10J3/66—Processes with decomposition of the distillation products by introducing them into the gasification zone
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
  • C10K1/00—Purifying combustible gases containing carbon monoxide
  • C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
• • 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
  • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
  • C10G2300/10—Feedstock materials
  • C10G2300/1003—Waste materials
• • 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
  • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
  • C10G2300/10—Feedstock materials
  • C10G2300/1011—Biomass
• • 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
  • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
  • C10G2300/40—Characteristics of the process deviating from typical ways of processing
  • C10G2300/4006—Temperature
• • 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
  • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
  • C10G2300/40—Characteristics of the process deviating from typical ways of processing
  • C10G2300/4012—Pressure
• • 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
  • C10J2300/0946—Waste, e.g. MSW, tires, glass, tar sand, peat, paper, lignite, oil shale
• • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
  • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
  • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
  • Y02P30/00—Technologies relating to oil refining and petrochemical industry
  • Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock

Definitions

• thermal cracking is cooling and cleaning of the hot synthesis gas. Due to a combination of tar and coke formation in practice, no coolers can be installed to recover heat and wet gas cleaning equipment is required. Therefore, the thermal efficiency of current thermal cracking processes is low and contaminated waste water is produced.
• the current thermal cracking systems and processes are not suitable to integrate novel technologies such as oxygen membranes and fuel cells, due to the tar content and the presence of salt vapour. Therefore extra heating/cooling and gas treatment equipment is required.
• a system for the thermal conversion of carbon based materials into combustible oil and/or gas said system comprises:
• said third reactor is operated at a temperature of 30°C to 80°C, preferably 35°C to 60°C, a hydrogen pressure of 200 to 300 mbar, preferably 225 to 275 mbar and an oxygen pressure of 10 ⁇ 5 to 10 ⁇ 9 mbar, preferably 10 ⁇ 6 to 10 ⁇ 8 ;
• a fourth moving bed reactor connected to said at least one outlet for carbon comprising solid material for stabilizing carbon in said solid material through conversion of gaseous materials, said fourth moving bed reactor comprises at least one intake, said at least one intake comprises at least one inlet for receiving said carbon comprising solid material and at least one discharge end, said at least one discharge end comprises at least one outlet for stabilized carbon comprising solid material, said fourth moving bed reactor is operated at a temperature of 550°C to 650°C, preferably 575°C to 625°C, a
• the present inventors have surprisingly discovered that a high quality oil and/or gas is obtained when thermal decomposition of carbon based materials is performed with the present system. Through using a series of separate reactors, in a specific order, the process conditions for each subprocess can be optimized. This results in an
• the present first fluid bed reactor for thermal cracking may also be designated as a reactor for thermal cracking or thermal cracker.
• Thermal cracking is a refining process in which heat and pressure are used to break down, rearrange, or combine carbon molecules.
• fuels and heavy oils were heated under pressure in large drums until they cracked into smaller molecules.
• the advantage of using a fluid bed reactor is the ease of maintaining a uniform temperature through the cracking reactor. This uniform temperature avoids the appearance of hot spots.
• the fluid bed reactor may comprise a Lewis acid.
• the fluid bed reactor is heated by hot gas from said fourth moving bed reactor.
• Fractionation is a separation process in which a mixture is divided in a number of desired fractions, wherein the composition of the fraction changes according to their gradient.
• the present third reactor separates and
• present fifth fluid bed reactor as used in the present context may also be denoted as quenching reactor or chemical quench.
• the fifth fluid bed reactor has a double role: gasification of the stabilised carbon
• Present sixth reactor may, according to the present invention, also be denoted as gasification reactor or gasifier.
• Gasification is a process that converts carbon based materials into carbon monoxide and hydrogen. This resulting gas mixture is so called synthesis gas or syngas. Gasification is characterized by its high temperatures which distinguished from for example biological processes.
• the first fluid bed reactor is connected through at least one inlet for receiving the carbon based materials with a dryer.
• the dryer comprises at least one inlet for receiving solid carbon based materials, at least one outlet for transporting dried solid carbon based materials into the first fluid bed reactor and at least one outlet for
• the first fluid bed reactor is connected through at least one inlet for receiving said carbon based materials with an homogeniser.
• the present homogeniser comprises at least one inlet for receiving liquid carbon based materials and at least one outlet for transporting homogenised liquid carbon based materials into the first fluid bed reactor.
• the present system comprises an oxygen membrane between the third reactor and the sixth reactor for oxygenation and/or oxidation of the non-condensed gas.
• residence time in the third reactor is 1 to 5 seconds
• the residence time in the fourth moving bed reactor is 180 to 240 minutes
• the residence time in the fifth fluid bed reactor is 30 to 120 minutes
• the residence time in the sixth reactor is 1 to 5 seconds.
• Figure 3 shows a system for the thermal cracking of a hydrocarbons comprising mass, comprising:
• a second cracking device connected with the discharge of the first cracking device (4) for the thermal separation of the charred product flow originating from the first cracking device in at least a heavy liquid fraction and a rest fraction, said second cracking device (4) comprising second heating means for heating the charred product flow,
• the process is characterized by leading hot synthesis gas from the second part of the process, the gasifier, to the third part of the process, the chemical quench (3) , where the hot synthesis gas gasifies the stablised char from the saturator (1) .
• This reaction is endothermic and
• the chemical quench (3) is a closed vessel fed with stabilised char that was treated in the saturator (1) . Because the stabilized char does not release liquid hydrocarbons, the synthesis gas practically does not contain any tar. The char is reduced to ashes and discharged from the vessel of the chemical quench.
• said system comprises the steps of:
• step B Further separating of the mass during step B) in a reducing atmosphere.
• step H Further heating the mass during step H) to a temperature of between 500°C and 800°C, preferably between 500°C and 600°C.
• the light fraction has a condensation temperature lower than 150°C.
• step B heating the mass during step B) to a temperature of between 500°C and 800°C, preferably between 550°C and 650°C.
• step D) during a time frame of between 0 to 10 seconds, preferably between 0 to 1 second.
• the heavy liquid fraction having a condensation temperature of between 150°C en 600°C.
• step L performing the gasification according to step L) at a temperature of between 500°C and 900°C, preferably between 700°C and 800°C.
• a device (2) connected with the discharge of the separation to a first gasification device for gasification at least a part of the heavy liquid fraction from the separation device originating in a first gaseous fraction, said primary gasification device comprising second heating means, second gasification device a connected with the discharge of the first gasification device for gasification, using the first gaseous fraction, at least a part of rest fraction formed the in the separation device in a second gaseous fraction, said second gasification device being provided with a discharge for discharging at least a part of the first gaseous fraction and at least a part of the second gaseous fraction.
• the separation device and the second gasification device are part of the same device.
• the system comprises administration means connected with the discharge of the first gasificaiton device for administrating the first gaseous fraction to the second
• the discharge for the discharging of at least a part of the first gaseous fraction and at least a part of the second gaseous fraction is accommodated in the upper section of the second gasification device.
• the second gasification device and the separation device form part of the same device.
• step D the heating of the heavy liquid fraction during step D) to a temperature between 1100 °C and 1500 °C, preferably between 1200 °C and 1400 °C.
• the distillation device (1) comprises heating means for the heating of the in the distillation lead product flow.
• step C) within a timeframe of
• step B 1 - 10 seconds after step B) initially is performed.
• steps B) , C) , D) being repeated at least one time after step F) is performed.
• the gasification device for the conversion of the combustible material in to a product gas and a rest fraction, in which the gasification device has at least one first discharge for the discharging of the product gas, and at least one second discharge for the discharging of the rest fraction,
• Figure 1 shows a first fluid bed reactor (1) for thermal cracking of sludges, liquids and/or solids
• the first fluid bed reactor (1) produces hot effluent vapour and gas which is transported to a second vapour wash reactor (2) .
• the remaining carbon comprising solid materials are transported to a fourth moving bed reactor (4) and remaining metals and minerals are discharged from the system and collected.
• the hot effluent vapour and gas are in the second vapour wash reactor (2) subjected to the conditions:
• the third reactor (3) produces combustible oil and non-condensed gas.
• the combustible oil is discharged (106) from the system and collected.
• the non-condensed gas is transported (107) to an oxygen membrane (10) .
• the non-condensed gas is in the oxygen membrane (10) subjected to the conditions:
• the oxygen membrane (10) produces oxygenated gas which is transported (108) to a sixth reactor (6) for gasification .
• the sixth reactor (6) produces processed gas which is transported (109) to a fifth fluid bed reactor (5) for cooling processed gas and gasification of stabilized carbon comprising solid material.
• the processed gas is in the fifth fluid bed reactor (5) subjected to the conditions:
• the fifth fluid bed reactor (5) produces cooled gas and gasified stabilized carbon comprising solid
• the gas is transported (110) via a fourth moving bed reactor (4) and the first fluid bed reactor (1) to a gasfilter (9).
• the gasified stabilized carbon comprising solid material is transported (111) to the first fluid bed reactor ( 1 ) .
• the gasfilter produces combustible gas and filter dust.
• the combustible gas and filter dust are discharged (112 and 113 respectively) from the system and collected.
• the fourth moving bed reactor (4) produces stabilized carbon comprising solid material which is transported (114) to the fifth fluid bed reactor (5)
• the dryer (7) receives solid carbon based materials. These solid carbon based materials are in dryer subjected to the conditions:
• the homogeniser (8) receives liquid or semi-liquid carbon based materials. These liquid or semi-liquid carbon based materials are in the homogenizer (8) subjected to the conditions :
• the homogenizer (8) produces homogenized liquid carbon based materials which are transported (117) to the first fluid bed reactor (1) .
• the calorific value of the synthesis gas obtained by the system according to the example was 5.1 MJ/Nm 3 .
• the combustible oil obtained in the above example has a good quality, as is further elucidated by Figure 2 which shows a GCMS analysis of the combustible oil obtained.

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• Chemical & Material Sciences (AREA)
• Engineering & Computer Science (AREA)
• Oil, Petroleum & Natural Gas (AREA)
• Organic Chemistry (AREA)
• Combustion & Propulsion (AREA)
• Chemical Kinetics & Catalysis (AREA)
• General Chemical & Material Sciences (AREA)
• Life Sciences & Earth Sciences (AREA)
• Wood Science & Technology (AREA)
• Processing Of Solid Wastes (AREA)
• Carbon And Carbon Compounds (AREA)

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• 2010
  • 2010-12-16 WO PCT/EP2010/069881 patent/WO2012010223A1/en active Application Filing
  • 2010-12-16 US US13/809,891 patent/US20130118075A1/en not_active Abandoned
  • 2010-12-16 EP EP10803071.9A patent/EP2596083A1/de not_active Withdrawn
  • 2010-12-16 BR BR112013001461A patent/BR112013001461A2/pt not_active IP Right Cessation

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