WO2012011803A1 - System and method for cracking a pyrolysable mass, in particular hydrocarbons - Google Patents

System and method for cracking a pyrolysable mass, in particular hydrocarbons Download PDF

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Publication number
WO2012011803A1
WO2012011803A1 PCT/NL2010/050464 NL2010050464W WO2012011803A1 WO 2012011803 A1 WO2012011803 A1 WO 2012011803A1 NL 2010050464 W NL2010050464 W NL 2010050464W WO 2012011803 A1 WO2012011803 A1 WO 2012011803A1
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WO
WIPO (PCT)
Prior art keywords
cracking
distillation
mass
discharge
fraction
Prior art date
Application number
PCT/NL2010/050464
Other languages
French (fr)
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/NL2010/050464 priority Critical patent/WO2012011803A1/en
Priority to BR112013001461A priority patent/BR112013001461A2/en
Priority to EP10803071.9A priority patent/EP2596083A1/en
Priority to US13/809,891 priority patent/US20130118075A1/en
Priority to PCT/EP2010/069881 priority patent/WO2012010223A1/en
Publication of WO2012011803A1 publication Critical patent/WO2012011803A1/en

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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
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B55/00—Coking mineral oils, bitumen, tar, and the like or mixtures thereof with solid carbonaceous material
    • 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
    • C10G2300/80—Additives
    • C10G2300/805—Water
    • C10G2300/807—Steam
    • 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 cracking a pyrolysable mass, in particular hydrocarbons.
  • the invention also relates to a method for cracking a pyrolysable mass, in particular hydrocarbons, preferably by using said system according to the invention,
  • biomass and waste containing also other non-biomass materials as plastics and synthetic rubbers, are heated in a closed vessel or chamber, the molecular structure
  • the products of this process are combustible gass.es at ambient temperature, such as hydrogen and carbon monoxide, liquid products, as a variety of hydrocarbons and tar, and charred material.
  • This process, thermal cracking is a well known process and also known as pyroiysis .
  • thermal cracking is a well known process and also known as pyroiysis .
  • the production of gaseous products, liquid products or the charred product is optimised in both quality and quantity .
  • the quality and yield of the liquid products depends on the residence time, the partial hydrogen pressure, the temperature in the thermal cracking process and the post processing, such as distillation.
  • the main objective is to prevent the formation of secondary cracking products and achieve water abstraction (catalysed by acid minerals such as sand or customary cracking catalyst) and saturation of unstable cracking products by hydrogen.
  • the liquid products are for the greater part a variety of hydrocarbons. If the residence time is to long, a Large part of these
  • hydrocarbons will further react to gaseous substances at ambient temperature ana carbon. This will decrease the yield of the liquid products.
  • the variety of these hydrocarbons will convert to more heavy hydrocarbons, such as tar, that, will increase the viscosity, and
  • the object can be achieved by providing a system according to claim 1 and a method according to claim 7.
  • the method according to the invention overcomes this dilemma by a fast removal of the vapours from the thermal cracking process (at temperature of typically 300 °C to ' 600 °C, preferably 400 °C) and directly introducing these vapours into the distillation process and separating the heavy liquid fraction (condensation temperature of typically 300 °C to 600 °C, preferably between 350 ⁇ 0 and 400 °C) containing dust particles, and feeding this fraction back to the thermal cracking process, hence increasing residence time of this fraction for further cracking into gasses and liquid products with desired, qualities.
  • the heavy liquid fraction can also be tapped to be used for several purposes. In this case the heavy liquid fraction is also separated from the oil fraction.
  • the (lighter) liquid products are to ' be used as boiler fuels or transportation fuels .
  • the invention disclosed in this description is a method for the yield of hydrocarbons from a thermal
  • the residue is fed back to the thermal cracking process or can be tapped directly as a product if desirable.
  • This fraction also contains dust particles, which are carried by the gas flow into the distillation process. Also these particles are returned to the thermal cracking process or are tapped.
  • the light liquid fraction is an oil fraction that does therefore not contain dust particles and can therefore be used as an engine or boiler fuel.
  • the invention leads to an optimal yield of liquid products as an oil fraction, not acid, insoluble in water and a heating value iLHV) of 30-48 MJ/kg, a high quality in respect to the use of boiler or transportation fuels.
  • figure 1 shews an schematic view of a system according to the invention.
  • Material preferably dried, is fed into a thermal cracking process ( 1) , possibly heated In the presence of reducing gas (a mixture of hydrogen, carbon monoxide and/or steam) and acid minerals such as sand and/or customary cracking catalyst to a temperature between 200 °C and 700 ° ' C in one or two phases.
  • reducing gas a mixture of hydrogen, carbon monoxide and/or steam
  • acid minerals such as sand and/or customary cracking catalyst
  • the products that are formed are a mixture of gasses, at ambient temperature, liquid products and char.
  • the gasses and liquid products that are in vapour state in the thermal cracking process ! 1 ) are directly fed to a distillation process (2) . This prevents the molecules from disintegrating any further into smaller molecules, hence giving an undesired high gas yield.
  • the invention is the quick removal of the gases and liquid products that are in vapour state in the thermal cracking process ⁇ 1 ⁇ , directly to a distillation process (2),
  • the hold up time of the removal is with a typical hold up time of 1 to 10 seconds and preferably 2 seconds.
  • distillation process separates by the difference in
  • condensation temperatures, the thermal cracking products in three fractions, a gaseous fraction, a light liquid and a heavy liquid The gaseous fraction is separated in the distillation process (2) with a minimum condensation temperature between ambient to 150 °C, preferable 100 °C. This prevents any water condensing and gives a light liquid without any water.
  • the heavy liquid is separated in the distillation process (2) with a condensation temperature of typically 150 °C to 600 °C, preferably between 200 and 400 °C. This heavy liquid contains dust particles and has a high viscosity, which are undesired properties for a boiler or transportation fuels.
  • the light liquid contains
  • the distillation conditions can be adjusted to meet specifications for boiler fuels or transportation fuel.
  • the liquid products are insoluble in water, are neutral and have a heating value (LHV) of 35-45 MJ/kg, depending of the composition of the input.
  • LHV heating value
  • the LHV of oil, produced from wood was found to have a LHV of 35,5 MJ/kg
  • the LHV of oil produced from a mixture of waste plastics and paper was found to have a LHV of 40 MJ/kg.
  • the LHV of gasoline produced from a mixture polyoief in' " s was found to have a LKV of 44 MJ/kg, the gasoline showed to be predominantly paraffinic .
  • Characteristic of this invention is leading the heavier liquid fraction at least partially back into the thermal crackinq process. By leading the heavier liquid fraction back to the thermal cracker the residence time of the heavier liquid fraction is increased, allowing further crackinq of the heavier liquid fraction, Also dust
  • the above described thermal cracking process can be operated both as a continuous process and as a batch process .
  • Preferable in the method according to the invention is the quick removal of the gasses and liquid products that are in vapour state in the thermal cracking process (1), directly to a distillation process (2) .
  • the gasses and liquid products that are in vapour state are separated by distillation in a a gaseous fraction, a light liquid and a heavier liquid.
  • Characteristic of this method is leading the heavier fraction at least partially back inLo the thermal cracking process (1) therefore controlling of residence time of heavy liquid in the thermal cracking process (1) by separating this fraction from the rest of the liquid traction from the thermal cracking process (1) by
  • distillation process (2) The heavy liquid is fed back to the thermal cracking process, where its hydrocarbon molecules disintegrate to a gaseous fraction, desired light liquid and carbon particles.
  • Preferable in the method according to the invention is the production of a liquid product neutral and insoluble in water with a heating value of 30 - 49 MJ/kg in an adjustable boiling range (gasoline though heavy gasoil) from a thermal cracking process, integrated with a
  • the liquid product does not contain liquids that would give a high viscosity, water or dust particles.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Materials Engineering (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Wood Science & Technology (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

When fossil fuels (as for example coal and tar sand), biomass and waste, containing also other non-biomass materials as plastics and synthetic rubbers, are heated in a closed vessel or chamber, the molecular structure disintegrates. The invention relates to an improved system for cracking a pyroiysable mass, in particular hydrocarbons. The invention also relates to a method for cracking a pyroiysable mass, in particular hydrocarbons, preferably by using said system according to the invention.

Description

SYSTEM AND METHOD FOR CRACKING A PYROLYSABLE MASS , IN
PARTICULAR HYDROCARBONS
The invention relates to a system for cracking a pyrolysable mass, in particular hydrocarbons. The invention also relates to a method for cracking a pyrolysable mass, in particular hydrocarbons, preferably by using said system according to the invention,
When fossil fuels {as for example coal and tar sand), biomass and waste, containing also other non-biomass materials as plastics and synthetic rubbers, are heated in a closed vessel or chamber, the molecular structure
disintegrates . The products of this process are combustible gass.es at ambient temperature, such as hydrogen and carbon monoxide, liquid products, as a variety of hydrocarbons and tar, and charred material. This process, thermal cracking, is a well known process and also known as pyroiysis . For different objectives at different thermal cracking process designs the production of gaseous products, liquid products or the charred product is optimised in both quality and quantity .
The quality and yield of the liquid products depends on the residence time, the partial hydrogen pressure, the temperature in the thermal cracking process and the post processing, such as distillation. To obtain the desired quality, the main objective is to prevent the formation of secondary cracking products and achieve water abstraction (catalysed by acid minerals such as sand or customary cracking catalyst) and saturation of unstable cracking products by hydrogen. The liquid products are for the greater part a variety of hydrocarbons. If the residence time is to long, a Large part of these
hydrocarbons will further react to gaseous substances at ambient temperature ana carbon. This will decrease the yield of the liquid products. However, when the residence time of the liquid products is too short, the variety of these hydrocarbons will convert to more heavy hydrocarbons, such as tar, that, will increase the viscosity, and
therefore have a negative impact on the quality of the liquid product for use as a boiler: or transportation fuel.
Known, thermal cracking and pyroiysis processes produce liquid fractions, but most use it as a fuel to heat the different reactors {patent EP1647589, W09744-410) , The quality of the liquid fractions is poor, due to their high acidity and their solubility in water. With a process in one patent (US 4-983278} found liquid fractions are produced and distilled in different fractions to obtain different liquid products.
It is an object of the invention to provide a relatively efficient system and method for converting a pyroiysabie mass at least partially into liquid products.
The object can be achieved by providing a system according to claim 1 and a method according to claim 7. The method according to the invention overcomes this dilemma by a fast removal of the vapours from the thermal cracking process (at temperature of typically 300 °C to '600 °C, preferably 400 °C) and directly introducing these vapours into the distillation process and separating the heavy liquid fraction (condensation temperature of typically 300 °C to 600 °C, preferably between 350 ΰ0 and 400 °C) containing dust particles, and feeding this fraction back to the thermal cracking process, hence increasing residence time of this fraction for further cracking into gasses and liquid products with desired, qualities. The heavy liquid fraction can also be tapped to be used for several purposes. In this case the heavy liquid fraction is also separated from the oil fraction. The (lighter) liquid products are to' be used as boiler fuels or transportation fuels .
The invention disclosed in this description is a method for the yield of hydrocarbons from a thermal
cracking reaction of combustible 'materials such as coal, biomass and waste . The thermal cracking is operated
typically at 300 - 600 °C at elevated temperature. With this method the products from a thermal cracking process are, removed and then fed to a distillation process within a hold-up time of typically 1 to 10 seconds, preferably 2 seconds. In the distillation process the products of the thermal cracking process are separated into three
fractions, a gaseous fraction, a light liquid fraction) and a heavy liquid fraction. The residue is fed back to the thermal cracking process or can be tapped directly as a product if desirable. This fraction also contains dust particles, which are carried by the gas flow into the distillation process. Also these particles are returned to the thermal cracking process or are tapped. The light liquid fraction is an oil fraction that does therefore not contain dust particles and can therefore be used as an engine or boiler fuel. The invention leads to an optimal yield of liquid products as an oil fraction, not acid, insoluble in water and a heating value iLHV) of 30-48 MJ/kg, a high quality in respect to the use of boiler or transportation fuels.
The invention is illustrated by way of the following non-limitative example, wherein:
figure 1 shews an schematic view of a system according to the invention.
Material, preferably dried, is fed into a thermal cracking process ( 1) , possibly heated In the presence of reducing gas (a mixture of hydrogen, carbon monoxide and/or steam) and acid minerals such as sand and/or customary cracking catalyst to a temperature between 200 °C and 700 °'C in one or two phases. 'The products that are formed are a mixture of gasses, at ambient temperature, liquid products and char. The gasses and liquid products that are in vapour state in the thermal cracking process ! 1 ) are directly fed to a distillation process (2) . This prevents the molecules from disintegrating any further into smaller molecules, hence giving an undesired high gas yield.
Preferable in the system according to the
invention is the quick removal of the gases and liquid products that are in vapour state in the thermal cracking process {1} , directly to a distillation process (2), The hold up time of the removal is with a typical hold up time of 1 to 10 seconds and preferably 2 seconds. The
distillation process separates by the difference in
condensation temperatures, the thermal cracking products in three fractions, a gaseous fraction, a light liquid and a heavy liquid. The gaseous fraction is separated in the distillation process (2) with a minimum condensation temperature between ambient to 150 °C, preferable 100 °C. This prevents any water condensing and gives a light liquid without any water. The heavy liquid is separated in the distillation process (2) with a condensation temperature of typically 150 °C to 600 °C, preferably between 200 and 400 °C. This heavy liquid contains dust particles and has a high viscosity, which are undesired properties for a boiler or transportation fuels. The light liquid contains
hydrocarbons with a condensation temperature of minimal 100 °C to a maximum of 400 °C. The distillation conditions can be adjusted to meet specifications for boiler fuels or transportation fuel. The liquid products are insoluble in water, are neutral and have a heating value (LHV) of 35-45 MJ/kg, depending of the composition of the input. Thus, the LHV of oil, produced from wood was found to have a LHV of 35,5 MJ/kg, The LHV of oil produced from a mixture of waste plastics and paper was found to have a LHV of 40 MJ/kg. The LHV of gasoline produced from a mixture polyoief in'" s was found to have a LKV of 44 MJ/kg, the gasoline showed to be predominantly paraffinic .
Characteristic of this invention is leading the heavier liquid fraction at least partially back into the thermal crackinq process. By leading the heavier liquid fraction back to the thermal cracker the residence time of the heavier liquid fraction is increased, allowing further crackinq of the heavier liquid fraction, Also dust
particles are removed from the light liquid products. The heavier liquid fraction disintegrates into gaseous
products, the desired light liquid products and coked material .
The above described method of a thermal cracking process (1) with a distillation process (2) makes it possible to control the yield and quality of the liquid products for the use of boiler and transportation fuels.
The above described thermal cracking process can be operated both as a continuous process and as a batch process .
Preferable in the method according to the invention is the quick removal of the gasses and liquid products that are in vapour state in the thermal cracking process (1), directly to a distillation process (2) . The gasses and liquid products that are in vapour state are separated by distillation in a a gaseous fraction, a light liquid and a heavier liquid.
Characteristic of this method is leading the heavier fraction at least partially back inLo the thermal cracking process (1) therefore controlling of residence time of heavy liquid in the thermal cracking process (1) by separating this fraction from the rest of the liquid traction from the thermal cracking process (1) by
distillation process (2) . The heavy liquid is fed back to the thermal cracking process, where its hydrocarbon molecules disintegrate to a gaseous fraction, desired light liquid and carbon particles.
Preferable in the method according to the invention is the production of a liquid product neutral and insoluble in water with a heating value of 30 - 49 MJ/kg in an adjustable boiling range (gasoline though heavy gasoil) from a thermal cracking process, integrated with a
distillation process (25. Because the vapours of the thermal cracking process (1) condense at a temperature at which water does not condense, the oil fraction does not contain any water. With this method of production the liquid product (oil fraction) does not contain liquids that would give a high viscosity, water or dust particles.
It should, be noted that the above-mentioned embodiments illustrate rather than limit the invention, ana that those skilled in the art will be able to design many alternative embodiments without departing from the scope of the appended claims. In the claims, any reference signs placed between parentheses shall not be construed as limiting the claim. Use of the verb "comprise" and its conjugations does not exclude the presence of elements or steps other than those stated in a claim. The article "a" or "an" preceding an element does not exclude the presence of a plurality of such elements. The mere fact that certain measures are recited in mutually different dependent claims does not indicate that a combination of these measures cannot be used to advantage.

Claims

Claims
1. System for cracking a pyrolysable mass, particulary hydrocarbons, comprising:
- a cracking device for the thermal cracking of a pyrolysable mass,
- a distillation device connected with a discharge of the cracking device for the separation of a from the cracking device originating substantially gaseous flow of a product in at least one heavy liquid fraction and at least one light fraction, whereby at least one discharge of the distillation device is connected with the inlet of the cracking device for the leading back from the distillation device to the cracking device of at least one part of the heavy liquid fraction, and whereby the distillation device comprises at least a second discharge for discharging at least one light fraction.
2. System as claimed in claim 1,
characterized by
at least one second discharge of the distillation device is equipped for the discharge of at least one light liquid fraction and that at least one other second discharge of the distillation device is equipped for the discharge of at least one gaseous fraction.
3. System as claimed in claim 1 or 2,
characterized by
the cracking device comprises first heating means for the heating of the pyrolysable mass
4. System as claimed in any of the foregoing claims, characterized by
a distillation device comprising heating means for the heating of the in the distillation lead product flow.
5. System as claimed in any of the foregoing claims, characterized by the system comprises at least one closing device for closing the discharge of the cracking device from the inlet of the distillation device.
6. System as claimed in any of the foregoing claims, characterized by
the system comprises at least one second closing device for closing the discharge of the distillation device from the inlet of the cracking device.
7. Method for cracking of a pyrolysable mass, particularly hydrocarbons, preferably using the device as claimed in any of the claims 1 to 6, comprising the following steps :
A) leading of a pyrolysable mass into a cracking device,
B) at least partial pyrolysing of the mass by means of heating the mass in the cracking device whereby a
substantially gaseous product flow is formed,
C) leading of at least one part of the substantially gaseous product flow to the distillation device,
D) by means of distillation separating the product flow in the distillation unit in at least one heavy liquid fraction and at least one light fraction,
E) removing from the distillation device of at least on part of the light fraction, and
F) leading at least one part of the heavy liquid fraction from the distillation device to the cracking device of
8. Method according to claim 7,
characterized by
heating the pyrolysable mass to a temperature of between 200 °C and 700 °C, preferably between 300 °C en 600 °C.
9. Method according to claim 7 or 8,
characterized by pyrolysing of the mass during step B) in a reducing atmosphere .
10. Method according to claim 9,
characterized by
submitting the mass during the pyrolysing to a reducing substance that is formed by at leastone substance chosen from the group consisting of: hydrogen, carbon monoxide, and steam.
11. Method according to any of the claims 7 - 10, characterized by
performing step C) within a timeframe of 1 - 10 seconds after step B) initially is performed.
12. Method according to any of the claims 7 to 11, characterized by
a heavy liquid fraction having a condensation temperature that amounts between 150 - 600 °C.
13. Method according to any of the claims 7 - 12, characterized by
the light fraction having a condensation temperature being less than 150 °C.
14. Method according to any of the claims 7 - 13, characterized by
steps B) , C) , D) being repeated at least one time after step F) is performed.
PCT/NL2010/050464 2010-07-19 2010-07-19 System and method for cracking a pyrolysable mass, in particular hydrocarbons WO2012011803A1 (en)

Priority Applications (5)

Application Number Priority Date Filing Date Title
PCT/NL2010/050464 WO2012011803A1 (en) 2010-07-19 2010-07-19 System and method for cracking a pyrolysable mass, in particular hydrocarbons
BR112013001461A BR112013001461A2 (en) 2010-07-19 2010-12-16 system and method for thermal conversion of coal-based materials
EP10803071.9A EP2596083A1 (en) 2010-07-19 2010-12-16 System and method for thermal conversion of carbon based materials
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 (en) 2010-07-19 2010-12-16 System and method for thermal conversion of carbon based materials

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
PCT/NL2010/050464 WO2012011803A1 (en) 2010-07-19 2010-07-19 System and method for cracking a pyrolysable mass, in particular hydrocarbons

Publications (1)

Publication Number Publication Date
WO2012011803A1 true WO2012011803A1 (en) 2012-01-26

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN104479711A (en) * 2014-11-26 2015-04-01 湖南科技大学 Method for improving yield of pyrolysis coal tar of low-rank coals

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GB425679A (en) * 1933-07-19 1935-03-19 Ronald Holroyd Improvements in or relating to the destructive hydrogenation of carbonaceous materials
US4328088A (en) * 1980-09-09 1982-05-04 The Pittsburg & Midway Coal Mining Co. Controlled short residence time coal liquefaction process
US4587006A (en) * 1985-07-15 1986-05-06 Breckinridge Minerals, Inc. Process for recovering shale oil from raw oil shale
US4983278A (en) 1987-11-03 1991-01-08 Western Research Institute & Ilr Services Inc. Pyrolysis methods with product oil recycling
WO1997044410A1 (en) 1996-05-20 1997-11-27 Rti Resource Transforms International Ltd. Energy efficient liquefaction of biomaterials by thermolysis
US6657095B1 (en) * 1998-04-01 2003-12-02 Recycled Energy, L.L.C. Continuous temperature variance pyrolysis for extracting products from tire chips
EP1847589A1 (en) 2006-04-20 2007-10-24 The Procter and Gamble Company Bleach particle

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB425679A (en) * 1933-07-19 1935-03-19 Ronald Holroyd Improvements in or relating to the destructive hydrogenation of carbonaceous materials
US4328088A (en) * 1980-09-09 1982-05-04 The Pittsburg & Midway Coal Mining Co. Controlled short residence time coal liquefaction process
US4587006A (en) * 1985-07-15 1986-05-06 Breckinridge Minerals, Inc. Process for recovering shale oil from raw oil shale
US4983278A (en) 1987-11-03 1991-01-08 Western Research Institute & Ilr Services Inc. Pyrolysis methods with product oil recycling
WO1997044410A1 (en) 1996-05-20 1997-11-27 Rti Resource Transforms International Ltd. Energy efficient liquefaction of biomaterials by thermolysis
US6657095B1 (en) * 1998-04-01 2003-12-02 Recycled Energy, L.L.C. Continuous temperature variance pyrolysis for extracting products from tire chips
EP1847589A1 (en) 2006-04-20 2007-10-24 The Procter and Gamble Company Bleach particle

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN104479711A (en) * 2014-11-26 2015-04-01 湖南科技大学 Method for improving yield of pyrolysis coal tar of low-rank coals
CN104479711B (en) * 2014-11-26 2016-05-25 湖南科技大学 A kind of method that improves low-order coal pyrolyzing coal tar yield

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