WO2012011800A1 - Système et procédé de craquage thermique d'hydrocarbures comprenant une masse - Google Patents

Système et procédé de craquage thermique d'hydrocarbures comprenant une masse Download PDF

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Publication number
WO2012011800A1
WO2012011800A1 PCT/NL2010/000110 NL2010000110W WO2012011800A1 WO 2012011800 A1 WO2012011800 A1 WO 2012011800A1 NL 2010000110 W NL2010000110 W NL 2010000110W WO 2012011800 A1 WO2012011800 A1 WO 2012011800A1
Authority
WO
WIPO (PCT)
Prior art keywords
fraction
gasification
cracking
discharge
heating
Prior art date
Application number
PCT/NL2010/000110
Other languages
English (en)
Inventor
Jacob Hendrik Obbo Hazewinkel
Original Assignee
Rl Finance B.V.
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Rl Finance B.V. filed Critical Rl Finance B.V.
Priority to PCT/NL2010/000110 priority Critical patent/WO2012011800A1/fr
Priority to EP10803071.9A priority patent/EP2596083A1/fr
Priority to US13/809,891 priority patent/US20130118075A1/en
Priority to PCT/EP2010/069881 priority patent/WO2012010223A1/fr
Priority to BR112013001461A priority patent/BR112013001461A2/pt
Publication of WO2012011800A1 publication Critical patent/WO2012011800A1/fr

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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
    • 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
    • C10J3/58—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
    • 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
    • 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
    • C10J2300/094—Char
    • 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
    • C10J2300/0953—Gasifying agents
    • C10J2300/0956—Air or oxygen enriched air
    • 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
    • C10J2300/12—Heating the gasifier
    • C10J2300/1253—Heating the gasifier by injecting hot 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
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1861—Heat exchange between at least two process streams
    • C10J2300/1869—Heat exchange between at least two process streams with one stream being air, oxygen or ozone
    • 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
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1861—Heat exchange between at least two process streams
    • C10J2300/1884—Heat exchange between at least two process streams with one stream being synthesis gas
    • 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
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
    • 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

  • the invention relates to a system for thermal cracking of a hydrocarbons comprising mass.
  • the invention also relates to a method for thermal cracking of a
  • hydrocarbons comprising mass, preferably by using the system according to the invention.
  • thermal cracking is a basic known process, also known as
  • Thermal cracking is a technique that can be used to produce different products from biomass, waste and other combustible materials. With thermal cracking, gaseous products, liquid products and/or char can be obtained.
  • Gaseous products can be used as a fuel or as a feedstock for chemical processes as for example methanol production.
  • the liquid products could be used as a fuel for boilers or transportation, if the product has the desired properties.
  • Charred material can be used as boiler fuel, consumer' s coal for example for barbeques or reduction material.
  • Charring material makes the release of metals from for example electronics waste less complex and makes a higher yield of metals possible.
  • Gasification of biomass and waste has the objective to produce a combustible gas as a gaseous fuel and/or to process waste.
  • thermal cracking processes solve some mentioned processes but not all sufficiently. Some thermal cracking processes produce oil as well as synthesis gas. The yield however depends on the input and the process temperature, but not on the return of oil to the thermal cracking process.
  • This object can be achieved by providing a system according to claim 1 and by providing a method according to claim 14. With the process the quality and quantity of the produced liquid products can be controlled and varied for the production of products in different qualities and quantities, and the synthesis gas produced, contains practically no tar.
  • figure 1 shows an schematic view of a system according to the invention.
  • the exemplary embodiment of the invention shows a schematic view of an improved thermal cracking process in which the quality and quantity of gaseous, liquid and solid products from solid combustible material as biomass, waste, fossil fuel and plastics is controlled and optimised.
  • Biomass, waste or other combustible materials are processed in a thermal cracking process (2) and a distillation process (3), to retrieve a defined quality and quantity of gaseous and liquid products.
  • the liquid products when regarded as residue, are gasified for the production of synthesis gas using charred input material.
  • the first and main liquid product is the liquid fraction, from the distillation process of the thermal cracking process (2) .
  • the liquid fraction is a mixture of
  • the liquid fraction can be used as a boiler or transportation fuel.
  • the second liquid product is the heavy liquid fraction from the distillation process. This fraction is separated in the distillation process (3) with a condensation temperature of typically 300 °C to 600 °C, preferably between 350 and 400 °C. This liquid contains dust particles and has a high viscosity. This fraction can be returned to the thermal cracking process (2), or can be tapped of to use as a heavy bunker fuel or for the
  • the third fraction is a mixture of hydrocarbons that are formed by heating unstable char in the saturator (4) to typically 500 °C to 800 °C, preferably 600 °C. This fraction can be described as a tar. It can be fed to the gasifier (5) or tapped of for
  • the solid product the mentioned combination could make if desired is the charred feedstock, further referred to as char.
  • the char is formed in the thermal cracking process (2) and heated in the saturator (4) typically between 500 °C to 800 °C, preferably 600 °C, and consists of carbon and possible non-organic material as for example metals and stone, depending on the feedstock.
  • the input of the process are all combustible materials that can be thermally cracked, such as biomass, waste and plastics. If necessary the materials are dried in the storage and drier (1) before they are fed to the thermal cracking process (2) .
  • the material is fed into a thermal cracking process, where it is heated in absence of air or any source of oxygen, to a temperature between 200 °C and 700 °C in one or two phases.
  • the thermal cracking process operates in combination with a distillation process (3) .
  • the products that are formed are a mixture of gasses, at ambient temperature, a liquid fraction and charred solid input material.
  • the gasses and liquid products that are in vapour state in the thermal cracking process (2) are directly fed to a . distillatio process (3) with a typical hold up time of 1 to 10 seconds and
  • the distillation process (3) separates by the difference in condensation temperatures the products obtained by thermal cracking in three fractions, a gaseous fraction, a light liquid fraction and a heavy liquid fraction.
  • the gaseous fraction has a condensation
  • the liquid fraction consists of hydrocarbons with a boiling temperature typical between 150 °C and 350 °C. The properties of this liquid are sufficient as a ' (half-) product as a boiler or transportation fuel.
  • the heavy liquid fraction is separated in the distillation process (3) with a condensation temperature of typically 300 °C to 600 °G, preferably between 350 and 400 °C. By leading this heavy liquid fraction into the thermal cracking process (2), the residence time of this fraction is increased, allowing further disintegration of the heavier organic molecules .
  • the thermal cracking process (2) is heated by a coil in which synthesis gas flows with a temperature of 500 °C.
  • the heavy liquid fraction from the distillation process (3) can be tapped of for the
  • the charred output can be extracted for different applications as products or half products for other processes.
  • the char is transported to the saturator (4).
  • the saturator (4) combined with the gasifier and the chemical quench (6), transforms the char with the heavy fraction from the saturator (4) in practical tar free synthesis gas.
  • the heavy fraction with a high condensing temperature is removed from the charred material.
  • the heavy liquid fraction is regarded as tar that could cause clogging of the synthesis gas for example pipes and engines.
  • the heavy Liquid fraction is gasified with the gaseous products from the distillation process of the thermal cracking process (2) at a temperature of typically 1200 °C to 1400 °C.
  • the char form the saturator (4) is transported to the chemical quench (6), where it is gasified by the synthesis gas from the gasifier.
  • the chemical quench (6) the carbon dioxide and water in the synthesis gas react with the carbon of the char, forming carbon monoxide and hydrogen. This reaction is endothermic.
  • the temperature of the synthesis gas therefore decreases from a temperature of typically 1200 °C to 1400 °C to a temperature typically 500 °C to 800 °C, preferably 600 °C, depending on the choice of operation. Because the treated 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 (6) via a water lock.
  • the heavy liquid fraction from the saturator (4) can, however, also be sent to the thermal cracking process (2) in order to achieve further residence time.
  • the hydrocarbons of the heavy fraction from the saturator (4) disintegrates into lighter fractions. These lighter fractions are then separated in the distillation into a gaseous fraction, a liquid fraction and a heavy liquid fraction. If desired, this heavy liquid fraction can also be tapped of for the extraction of chemicals.
  • the gaseous fraction is a mixture of substances with a condensation temperature between ambient to 150 °C, preferable 110 °C.
  • the gaseous fraction contains water vapour and is in many cases therefore not suitable as a fuel for gas engines.
  • the gaseous fraction is therefore fed to the gasifier with the heavy liquid fraction from the saturator (4) .
  • the synthesis gas from the chemical quench (6) has a temperature of typically 500 °C to 800 °C, preferably 600 °C.
  • This synthesis gas practically does not contain any heavy liquid fraction that as a tar could cause problems as for example clogging pipes and tubes as in for example the heating coils (8) .
  • the synthesis gas is lead as a heating gas through coils in firstly the saturator (4) and secondly the thermal cracking process (2), before the synthesis gas preheats the air for the gasifier (5) .
  • This invention is preferably characterised by using the hydrogen rich gas for transportation of instable hydrocarbons and acidulous hydrocarbons. With hydrogen rich gas as a drive gas these instable hydrocarbons and
  • In this invention is preferably characterised by the use of the produced synthesis gas to preheat the air (7) for gasification.
  • the above described process can be operated as a batch operation, using only one reactor for the thermal cracking of the in feed material, condensing the liquid fraction with a high condensing temperature from the char as in the saturator, followed b the gasification of this char by synthesis gas, air or oxygen.
  • the vapours from the thermal cracking in the batch reactor can be sent to an external distillation process for the separation in a gaseous fraction, a liquid fraction and a tar fraction.
  • the tar fraction can be sent back to the batch reactor that is in a stage of thermal cracking.
  • the heavy tar can be gasified externally or, if desired, tapped of for the thermal cracking in a new batch or for applications as bunker fuels or the extraction of chemicals.
  • the hot tarless synthesis gas f om the gasification of the char can be used the preheat gasification air or heat other batch reactors operating this process.
  • the invention is preferably characterised by the use of a thermal cracking process (2) and a method of tar free synthesis gas production, in order co obtain and controlled and optimised process of gaseous, liquid and solid products from solid combustible material as for example coal, biomass, waste and plastics, wherein the cracking process preferably comprises one or multiple aspects of the following aspects:
  • distillation process (3) into a gaseous fraction and the desired light liquid fraction.
  • the invention is preferably characterised by the possibility of operating the process as a batch process using only one reactor for the thermal cracking of the in feed material, condensing the liquid fraction with a high condensing temperature from the char as in the saturator, followed by the gasification of this char by synthesis gas, air or oxygen.
  • the vapours from the batch operation can be sent to any distillation process. Any tar fractions from this batch process can be tapped of for the thermal cracking in a new batch or for applications as bunker fuels or the extraction of chemicals.
  • the hot tarless synthesis gas from the gasification of the char can be used the preheat gasification air or heat other batch reactors operating this process.

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

Abstract

Un des objectifs de la gazéification et de la pyrolyse des matières combustibles telles que, par exemple, le charbon, une biomasse ou des déchets est la production d'un gaz combustible sous forme de carburant gazeux. L'invention concerne un système de craquage thermique d'hydrocarbures comprenant une masse. L'invention concerne également un procédé de craquage thermique d'hydrocarbures comprenant une masse, de préférence, à l'aide du système selon l'invention.
PCT/NL2010/000110 2010-07-19 2010-07-19 Système et procédé de craquage thermique d'hydrocarbures comprenant une masse WO2012011800A1 (fr)

Priority Applications (5)

Application Number Priority Date Filing Date Title
PCT/NL2010/000110 WO2012011800A1 (fr) 2010-07-19 2010-07-19 Système et procédé de craquage thermique d'hydrocarbures comprenant une masse
EP10803071.9A EP2596083A1 (fr) 2010-07-19 2010-12-16 Système et procédé de conversion thermique de matériaux à base de carbone
US13/809,891 US20130118075A1 (en) 2010-07-19 2010-12-16 System And Method For Thermal Conversion Of Carbon Based Materials
PCT/EP2010/069881 WO2012010223A1 (fr) 2010-07-19 2010-12-16 Système et procédé de conversion thermique de matériaux à base de carbone
BR112013001461A BR112013001461A2 (pt) 2010-07-19 2010-12-16 sistema e método para conversão térmica de materiais à base de carvão

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
PCT/NL2010/000110 WO2012011800A1 (fr) 2010-07-19 2010-07-19 Système et procédé de craquage thermique d'hydrocarbures comprenant une masse

Publications (1)

Publication Number Publication Date
WO2012011800A1 true WO2012011800A1 (fr) 2012-01-26

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Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4983278A (en) * 1987-11-03 1991-01-08 Western Research Institute & Ilr Services Inc. Pyrolysis methods with product oil recycling
US6084139A (en) * 1997-12-05 2000-07-04 Gibros Pec B.V. Method for processing waste or biomass material
US20070163176A1 (en) * 2005-07-28 2007-07-19 Choren Industries Gmbh Process and apparatus for the endothermic gasification of carbon
US20090062581A1 (en) * 2003-03-28 2009-03-05 Appel Brian S Methods and apparatus for converting waste materials into fuels and other useful products
EP2177590A1 (fr) * 2008-10-17 2010-04-21 Resetec Patent Sarl Procédé et appareil pour le dégazage d'un aliment comprenant des hydrocarbures et la gazéification d'un residue de dégazage

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4983278A (en) * 1987-11-03 1991-01-08 Western Research Institute & Ilr Services Inc. Pyrolysis methods with product oil recycling
US6084139A (en) * 1997-12-05 2000-07-04 Gibros Pec B.V. Method for processing waste or biomass material
US20090062581A1 (en) * 2003-03-28 2009-03-05 Appel Brian S Methods and apparatus for converting waste materials into fuels and other useful products
US20070163176A1 (en) * 2005-07-28 2007-07-19 Choren Industries Gmbh Process and apparatus for the endothermic gasification of carbon
EP2177590A1 (fr) * 2008-10-17 2010-04-21 Resetec Patent Sarl Procédé et appareil pour le dégazage d'un aliment comprenant des hydrocarbures et la gazéification d'un residue de dégazage

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