WO2012011799A2 - System and method for thermal cracking of a hydrocarbons comprising mass - Google Patents
System and method for thermal cracking of a hydrocarbons comprising mass Download PDFInfo
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- WO2012011799A2 WO2012011799A2 PCT/NL2010/000109 NL2010000109W WO2012011799A2 WO 2012011799 A2 WO2012011799 A2 WO 2012011799A2 NL 2010000109 W NL2010000109 W NL 2010000109W WO 2012011799 A2 WO2012011799 A2 WO 2012011799A2
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- WIPO (PCT)
- Prior art keywords
- fraction
- gasification
- mass
- gaseous fraction
- rest
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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
- C10G1/02—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by distillation
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
- C01B3/36—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using oxygen or mixtures containing oxygen as gasifying agents
-
- 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
-
- 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
- C10K3/00—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide
- C10K3/001—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by thermal treatment
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/025—Processes for making hydrogen or synthesis gas containing a partial oxidation step
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/08—Methods of heating or cooling
- C01B2203/0872—Methods of cooling
- C01B2203/0877—Methods of cooling by direct injection of fluid
-
- 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
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
- C10J2300/1603—Integration of gasification processes with another plant or parts within the plant with gas treatment
- C10J2300/1618—Modification of synthesis gas composition, e.g. to meet some criteria
-
- 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
- CN101007956 is a new example. It is an object of the invention to provide a relatively efficient system and method for thermal cracking of a hydrocarbons comprising mass.
- This hot synthesis gas is mixed with the stabilized char, for instance in a fluidized bed.
- the mix is cooled by the endothermic gasification of the stabilised char, thus producing more (higher calorific) synthesis gas at a
- figure 1 shows an schematic view of a system according to the invention.
- these hydrocarbons are gasified and converted into carbon monoxide, carbon dioxide, hydrogen and water vapour.
- the formed synthesis gas practically does not contain any tar.
- the synthesis gas from this gasification is sent to an other batch reactor that was operated as a saturator and is now operated as a chemical quench, by leading the synthesis gas through the batch reactor.
- This process is further preferably characterised by heating charred material in a closed vessel, the saturator (1), at a temperature of typically 500 °C to
- the tar of one batch reactor can be gasified at a
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Combustion & Propulsion (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- General Chemical & Material Sciences (AREA)
- Wood Science & Technology (AREA)
- Life Sciences & Earth Sciences (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Health & Medical Sciences (AREA)
- General Health & Medical Sciences (AREA)
- Inorganic Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Processing Of Solid Wastes (AREA)
Abstract
One of the objectives of gasification and pyrolysis of combustible matter as for example coal, biomass or waste is the production of a combustible gas as a gaseous fuel. The invention relates to a system for thermal cracking of a hydrocarbons comprising mass by first heating and separating a heavy liquid fraction from the mass, then gasifying the heavy liquid in a first gasification device at high temperature and finally gasifying the rest of the mass in a second gasification device by contacting the said mass with the gas obtained in the first gasification device. The invention also relates to a method for thermal cracking of a hydrocarbons comprising mass, preferably by using the system according to the invention.
Description
SYSTEM AND METHOD FOR THERMAL CRACKING OF
A HYDROCARBONS COMPRISING MASS
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.
One of the objectives of gasification and pyrolysis of combustible matter as for example coal, biomass or waste is the production of a combustible gas as a gaseous fuel. When combustible matter, possibly
containing also other non-biomass materials as plastics and synthetic rubbers, is heated in the absence of. oxygen, in a closed vessel or chamber, the molecular structure
disintegrates. The products of this process are combustible gases at ambient temperature, such as hydrogen and carbon monoxide, liquid products, as a variety of hydrocarbons and tar, and charred material. The gas/hydrocarbon/char ratio depends on the temperature. This process, thermal cracking is a basic known process, also known as pyrolysis
(typically operated at 400 - 500 °C, no or very less addition of a mixture of oxygen and air) or gasification (typically operated at 900 °C, insufficient addition, of oxygen and air for complete combustion) . Whereas pyrolysis (typical gas/hydrocarbon/char ratio of 10/50/40) is only slightly endothermic, the energy requirement of
gasification (typical gas/hydrocarbon/char ratio of 99/1/0) amounts to approx. 30% of the heating value of the input. Heat is supplied directly (by partial combustion or for instance adding hot sand) or indirectly by a heated surface.
One of the major problems with synthesis gas as a fuel from a thermal cracking process is the content of tar. When the synthesis gas is cooled the tar will give clogging problems in pipes, heat exchangers and impairs the trouble free operation of the gas users such as engines.
An other problem of gasification is the phenomenon that minerals and especially salts, present in the input will reach their softening point at temperatures above approximate 750 °C (high potassium content, typical for rice husks) through approximate 900 °C (typical for wood and mixed waste) , resulting in clogging of the gasifier equipment.
Yet another problem of gasification is the 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 gasification processes is low and contaminated waste water is produced.
The current gasification 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.
In many patents the problem of tar in the production of synthesis gas, or any kind of fuel gas from a pyrolysis or gasification process, is addressed. Apart from thermal cracking by adding oxygen or air, also steam reforming ( JP2007045857 ) , catalytic conversion (EP1577366) tar removal by fuel gas washing (JP56020398) and recycling the washed out tar back to the pyrolysis reactor
(EP1312662) are described as solutions in patents. Thermal cracking of tar is proposed in many patents of which
CN101007956 is a new example.
It is an object of the invention to provide a relatively efficient system and method for thermal cracking of a hydrocarbons comprising mass.
This object can be achieved by providing a system
5 according to claim 1, and by providing a method according to claim 7, the thermal energy obtained by the exothermal gasification of the heavy liquid fraction is used to gasify the residue fraction. The invention disclosed in this application is a process where tar free synthesis gas is
) produced using stabilized char produced from for example biomass or waste by for example a thermal cracking process, or using coal or coal products (for example coke), further to be named with the term "char". The char is stabilised by heating to release any volatile compounds, mostly
5 hydrocarbons. These volatile hydrocarbons are then, when the case with any other gaseous product from a pyrolysis or gasification process, gasified with (enriched) air or oxygen at a high temperature, typically between 1200 °C to 1400 °C, where all volatile hydrocarbons are converted to
) (low calorific) synthesis gas without the formation of
char. This hot synthesis gas is mixed with the stabilized char, for instance in a fluidized bed. The mix is cooled by the endothermic gasification of the stabilised char, thus producing more (higher calorific) synthesis gas at a
5 temperature of typically 700 °C to 800 °C. In the context of this application it is noted that the term "synthesis gas" is not restricted to carbon monoxide and hydrogen, by may also include e.g. nitrogen, water vapour, and carbon dioxide .
D The above described thermal cracking process can be operated both as a continuous process and as a batch process .
The invention is illustrated by way of the following non-limitative example, wherein:
figure 1 shows an schematic view of a system according to the invention.
The invention is a process that can be continuously operated in three major reactors. The first part is the saturator (1) where liquid hydrocarbons with a high condensing temperature are removed from the char. The second part is the gasifier (2) , an empty reactor providing a hold up time, where these liquid hydrocarbons, possible with other synthesis gas from the pyrolysis or gasification process, are gasified at a temperature of typically 1200 °C to 1400 °G. The third part is the chemical quench (3), where the hot synthesis gas of the gasifier (2) is used for the endothermic gasification of the char from the saturator (1) ·
The invention is preferably characterised by the removal of liquid hydrocarbons with a high condensing temperature from the char by external heating (4), the temperature of the char is increased to typically 500 °C to 800 °C, preferably 600 °C. At this temperature, liquid hydrocarbons with a high condensing temperature are released. These liquid hydrocarbons are regarded as tar that could cause clogging at applications as for example pipes and engines. The char is stabilised by releasing the liquid hydrocarbons at a high condensing temperatures. This process takes places in the saturator (1) .
The second part is the gasifier (2) , an empty reactor providing a hold up time, where these liquid hydrocarbons, possible with other synthesis gas from the pyrolysis or gasification process, are gasified at a temperature of typically 1200 °C to 1400 °C. At this high temperature and with a typical residence time of less than ■1 second, these hydrocarbons are gasified and converted into carbon monoxide, carbon dioxide, hydrogen and water vapour. The formed synthesis gas practically does not
contain any tar. However, due to the combustion a large part of the gas is converted into carbon dioxide.
The invention is preferably characterised 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 stabilised char from the saturator (1). This reaction is endothermic and therefore decreases the temperature of the synthesis gas to a temperature of typically approximate 700 °C to 800 °C depending on the choice of operation. The chemical quench (3) is a closed vessel fed with stabilised char that was treated in the saturator (1). Because the stabilised 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.
The invention of this process is preferably characterised by a batch wise operation in only one reactor. By external heating of char or coal in one batch reactor, to typically 500 °C to 800 °C, preferably 600 °C, liquid hydrocarbons with a high condensing temperature are released. After this treatment the char is gasified with synthesis gas that could contain char, or gasified with air or oxygen, in an operation that is described by the chemical quench in an continuous process. The synthesis gas form this batch process does not contain any tar. When more batch reactors are operated simultaneously, the tar of one batch reactor can be gasified at a temperature of typically 1200 °C to 1400 °C. At this high temperature and with a typical residence time of less than 1 second, these hydrocarbons are gasified and converted into carbon monoxide, carbon dioxide, hydrogen and water vapour. The formed synthesis gas practically does not contain any tar. The synthesis gas from this gasification is sent to an
other batch reactor that was operated as a saturator and is now operated as a chemical quench, by leading the synthesis gas through the batch reactor.
A preferable characteristic of this process is the production of tar free synthesis gas from a thermal cracking reaction as for example a gasification or
pyrolysis reaction, by the removal of liquid hydrocarbons with a high condensing temperature from any formed char by heating the char, and followed by gasifying this char with the hot synthesis gas produced by gasification of the tar. The product of this process is a tar free medium calorific gas with practically no tars.
This process is further preferably characterised by heating charred material in a closed vessel, the saturator (1), at a temperature of typically 500 °C to
800 °C, preferably 600 °C, and releasing hydrocarbons with a high condensation temperature such as tars.
This process is preferably characterised by gasifying of the released hydrocarbons in the gasifier (2) at a temperature of typically 1200 °C to 1400 °C, reducing al hydrocarbons to synthesis gas containing practically no ta .
This process is preferably characterised by the endothermic gasification of the stabilised char with the synthesis gas in the chemical quench (3), to a synthesis gas with practically no tars at a temperature of typically approx. 700 °C to 750 °C, resulting in the producing a tar free medium calorific gas with practically no tars, resulting in the prevention clogging of the equipment and resulting in increasing the overall thermal efficiency of the process.
The invention of this process is preferably characterised by a batch wise operation in only one reactor, by first external heating char or coal in one
batch reactor, to typically 500 °C to 800 °C, preferably 600 °C, to release liquid hydrocarbons with a high
condensing temperature, and secondly gasification with synthesis gas, air or oxygen, in an operation that is described by the chemical quench in an continuous process. In case more batch reactors are operated simultaneously, the tar of one batch reactor can be gasified at a
temperature of typically 1200 °C to 1400 °C. The synthesis gas from this gasification is sent to an other batch reactor that was operated as a saturator and is now operated as a chemical quench, by leading the synthesis gas through the batch reactor.
It should be noted that the above-mentioned embodiments illustrate rather than limit the invention, and 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
1. System for the thermal cracking of a hydrocarbons comprising mass, comprising:
a separation device for the thermal separation of a mass comprising hydrocarbons in at least a heavy liquid fraction and a rest fraction said separation device comprising first heating means for heating of mass,
a device 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 firs gaseous fraction and at least a part of the second gaseous fraction.
2. System as claimed in claim 1,
characterized in that
the separation device and the second gasification device are mirtually connected, and that the system comprises transportation means for the transportation of the rest fraction formed in the separation device to the second gasification device.
3. System as claimed in claim 1, characterized in that
the separation device and the second gasification device are part of the same device.
4. System as claimed in any of the foregoing claims, characterized in that
the second gasification device is provided with means for causing the first gaseous fraction to flow through the rest fraction.
5. System as claimed in claim 4,
characterized in that
the system comprises administration means connected with the discharge of the first gasificaiton device for administrating the first gaseous fraction to the second gasification device, whereby the administration means extend to the lower section of the second gasification device .
6. System as claimed in any of the foregoing claims, characterized by
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.
7. Method for the thermal cracking of a mass, comprising hydrocarbons, in particular using a system as claimed in any of claims 1 - 6, comprising the steps of:
A) leading a mass comprising hydrocarbons in to the
separation device,
B) separating by means of heating the mass in the
separation device in a heavy liquid fraction and a rest fraction, C) leading at least a part of the heavy liguid fraction to a first gasification device,
D) converting at least a part of the heavy liquid
fraction in a first gaseous fraction by means of heating the heavy liquid fraction,
E) leading at least a part of the first gaseous fraction to the second gasification device,
F) heating of the rest fraction in the second
gasification device by bringing the rest fraction into contact with at least a part of the first gaseous fraction, whereby at least a part of the rest fraction is converted into a second gaseous fraction, and
G) discharging at least a part of the first gaseous
fraction and least a part of the second gaseous fraction .
8. Method according to claim 7,
characterized in that
the second gasification device and the separation device form part of the same device.
9. Method according to claims 7 or 8,
characterized by
leading the first gaseous fraction during step F) through at least a part of the rest fraction.
10. Method according to claim 9,
characterized by
the fluidisation of at least a part of the rest fraction during step F) by the gaseous fraction.
11. Method according to one of the claims 7 to 10,
characterized by heating the mass during step B) to a temperature between 500 °C and 800 °C, preferably between 550 °C and 650 °C.
12. Method according to one of the claims 7 to 11, characterized by
performing step D) within a time frame of 0 to
10 seconds, preferably within 0 to 1 second.
13. Method according to one of the claims 7 to 12, characterized by
the condensation temperature of the heavy liquid, being between 150 °C and 600 °C.
14. Method according to one of the claims 7 to 13, characterized by
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.
15. Method according to one of the claims 7 to 14, characterized by
performing of the gasification according to step G) at a temperature between 500 °C and 900 °C, preferably between 700 °C and 800 °C.
16. Method according to one of the claims 7 to 15,
characterized by
the gaseous fraction comprising at least one substance selected from the group comprising carbon monoxide, carbon dioxide, and steam.
Priority Applications (5)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| PCT/NL2010/000109 WO2012011799A2 (en) | 2010-07-19 | 2010-07-19 | System and method for thermal cracking of a hydrocarbons comprising mass |
| 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/NL2010/000109 WO2012011799A2 (en) | 2010-07-19 | 2010-07-19 | System and method for thermal cracking of a hydrocarbons comprising mass |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| WO2012011799A2 true WO2012011799A2 (en) | 2012-01-26 |
| WO2012011799A3 WO2012011799A3 (en) | 2012-03-15 |
Family
ID=44624846
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| PCT/NL2010/000109 WO2012011799A2 (en) | 2010-07-19 | 2010-07-19 | System and method for thermal cracking of a hydrocarbons comprising mass |
Country Status (1)
| Country | Link |
|---|---|
| WO (1) | WO2012011799A2 (en) |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5620398A (en) | 1979-07-27 | 1981-02-25 | Hitachi Ltd | Electronic control tone arm |
| EP1312662A2 (en) | 2001-05-07 | 2003-05-21 | Cirad-Foret | Biomass gasification process, and apparatus, and their applications |
| EP1577366A2 (en) | 2004-03-14 | 2005-09-21 | Ozmotech Pty. Ltd. | Process for conversion of waste material to liquid fuel |
| JP2007045857A (en) | 2005-08-05 | 2007-02-22 | Nippon Steel Corp | Method and apparatus for purifying gasified gas |
| CN101007956A (en) | 2007-01-18 | 2007-08-01 | 上海交通大学 | Two-stage type biomass gasification stove aditus structure |
Family Cites Families (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR2457319A1 (en) * | 1979-05-22 | 1980-12-19 | Lambiotte Usines | PROCESS FOR COMPLETE GASIFICATION OF CARBONACEOUS MATERIALS |
| US4983278A (en) * | 1987-11-03 | 1991-01-08 | Western Research Institute & Ilr Services Inc. | Pyrolysis methods with product oil recycling |
| DE4404673C2 (en) * | 1994-02-15 | 1995-11-23 | Entec Recycling Und Industriea | Process for the production of fuel gas |
| NL1007710C2 (en) * | 1997-12-05 | 1999-06-08 | Gibros Pec Bv | Method for processing waste or biomass material. |
| DE102004053494B4 (en) * | 2004-10-28 | 2008-11-06 | Michael Prestel | Method and apparatus for converting energy using biomass |
| EP1696177A1 (en) * | 2005-02-28 | 2006-08-30 | Drechsler, Daniel | Integrated multifuel gasification process |
-
2010
- 2010-07-19 WO PCT/NL2010/000109 patent/WO2012011799A2/en active Application Filing
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5620398A (en) | 1979-07-27 | 1981-02-25 | Hitachi Ltd | Electronic control tone arm |
| EP1312662A2 (en) | 2001-05-07 | 2003-05-21 | Cirad-Foret | Biomass gasification process, and apparatus, and their applications |
| EP1577366A2 (en) | 2004-03-14 | 2005-09-21 | Ozmotech Pty. Ltd. | Process for conversion of waste material to liquid fuel |
| JP2007045857A (en) | 2005-08-05 | 2007-02-22 | Nippon Steel Corp | Method and apparatus for purifying gasified gas |
| CN101007956A (en) | 2007-01-18 | 2007-08-01 | 上海交通大学 | Two-stage type biomass gasification stove aditus structure |
Also Published As
| Publication number | Publication date |
|---|---|
| WO2012011799A3 (en) | 2012-03-15 |
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