US20130118075A1

US20130118075A1 - System And Method For Thermal Conversion Of Carbon Based Materials

Info

Publication number: US20130118075A1
Application number: US13/809,891
Authority: US
Inventors: Jacob Hendrik Obbo Hazewinkel
Original assignee: GET PATENT BV
Current assignee: GET PATENT BV
Priority date: 2010-07-19
Filing date: 2010-12-16
Publication date: 2013-05-16
Also published as: WO2012010223A8; BR112013001461A2; WO2012010223A1; EP2596083A1

Abstract

The present invention relates to a system for thermal conversion of carbon based materials into combustible oil and/or gas. More specifically, said system comprises: a first fluid bed reactor, a second vapour wash reactor, a third fractionation reactor, a fourth moving bed reactor, a fifth fluid bed reactor and a sixth gasification reactor.

Description

The present invention relates to a system for thermal conversion of carbon based materials. More specifically, the present invention relates to a system for thermal conversion of carbon based materials into combustible oil and/or gas. Further, the present invention relates to a method for thermal conversion of carbon based materials into combustible oil and/or gas. The present invention also relates to the use of the present system for thermal conversion of carbon based materials into combustible oil and/or gas.
One of the objectives of thermal conversion of carbon based, or carbon comprising matter, for example biomass, wood, forestry waste products, organic waste, agricultural waste products, plastics, tires, tar sand, industrial waste, municipal waste, airport waste, entertainment industry waste, harbour waste, hospital waste or reject coal, is the production of a combustible oil or gas, i.e. an oil or gas that can be used as a fuel source for engines, turbines, heating devices, steam devices etc.
When carbon based materials are heated under reduced oxygen pressure, such as in the absence of oxygen, in a closed vessel or chamber, the molecular structure of these carbon based materials disintegrates. As a result of this disintegration, combustible gasses such as hydrogen, methane and/or ethane are formed next to combustible oils comprising larger carbon chains.
The process of thermally disintegrating carbon based, or carbon comprising, materials under a reduced oxygen pressure is also designated as thermal cracking or pyrolysis.
Thermal cracking, or thermal disintegration or pyrolysis, of carbon comprising materials is a technique that can be used to convert these materials into valuable combustible oil and gas that subsequently can be used, for example, to power vehicles, generate electricity in turbines or as base products for chemical synthesis.
Problems associated with many thermal cracking processes are the design of a process capable of producing only one product, the liquids obtained from the thermal cracking process not having the desired properties, and the synthesis gas in many cases containing tar, giving clogging problems in various applications.
Another problem of thermal cracking, and especially 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 the known systems for the conversion of carbon based materials is large scale of the equipment required. Providing such a large scale system requires enormous investments and substantive installation times.
Yet another problem associated with 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.
In many prior art disclosures, 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, catalytic conversion, tar removal by fuel gas washing, and recycling the washed out tar back to a pyrolysis reactor are described as solutions.
Considering the above, there is a need in the art for a system and a method for thermal conversion of carbon based materials into combustible oil and/or gas obviating at least part, if not all, of the above problems.
Therefore, it is an object of the present invention, amongst other objects, to provide a system obviating at least part, if not all, of the above problems associated with conversion of carbon based materials into combustible oil and/or gas. This objective, amongst other objects, is met by a system as defined in the appended claim 1.
Specifically, this objective, amongst other objectives, is met by a system for the thermal conversion of carbon based materials into combustible oil and/or gas, said system comprises:

- a) a first fluid bed reactor for thermal cracking of said carbon based materials, said first fluid bed reactor comprises at least one intake, said at least one intake comprises at least one inlet for receiving said carbon based materials, at least one inlet for receiving processed solid materials and at least one inlet for receiving solids and oil, at least one discharge end, said at least one discharge end comprises at least one outlet for carbon comprising solid material, at least one outlet for metals and minerals, and at least one outlet for effluent vapour and gas, and said first fluid bed reactor is operated at a temperature of 350° C. to 450° C., preferably 375° C. to 425° C., a hydrogen pressure of 200 to 300 mbar, preferably 225 to 275 mbar and an oxygen pressure of 10⁻⁵to 10⁻⁹mbar, preferably 10⁻⁶to 10⁻⁸;
- b) a second vapour wash reactor connected to said outlet for effluent vapour and gas for washing effluent vapour and gas from said first fluid bed reactor, said second vapour wash reactor comprises at least one intake, said at least one intake comprises at least one inlet for receiving said effluent vapour gas and at least one discharge end, said at least one discharge end comprises at least one outlet for washed vapour and gas and at least one outlet for solids and oil connected to said inlet for solids and oil of said first fluid bed reactor for reintroducing said solids and oil into said first fluid bed reactor, and said second vapour wash reactor is operated at a temperature of 150° C. to 300° C., preferably 200° C. to 250° C., a hydrogen pressure of 200 to 300 mbar, preferably 225 to 275 mbar and an oxygen pressure of 10⁻⁵to 10⁻⁹mbar, preferably 10⁻⁶to 10⁻⁸;
- c) a third reactor connected to said outlet for washed vapour and gas for fractioning of said vapour and gas, said third reactor comprises at least one intake, said at least one intake comprises at least one inlet for receiving said washed vapour and gas, at least one discharge end, said at least one discharge end comprises at least one outlet for combustible oil and at least one outlet for non-condensed gas, and 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 10⁻⁵to 10⁻⁹mbar, preferably 10⁻⁶to 10⁻⁸;
  wherein said carbon comprising solid material from said first fluid bed reactor is reintroduced into said first fluid bed after been processed in
- d) 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 hydrogen pressure of 200 to 300 mbar, preferably 225 to 275 mbar and an oxygen pressure of 10⁻⁵to 10⁻⁹mbar, preferably 10⁻⁶to 10⁻⁸;
- e) a fifth fluid bed reactor connected to said at least one outlet for stabilized carbon comprising solid material, said fifth fluid bed reactor comprises at least one intake, said at least one intake comprises at least one inlet for receiving said stabilised carbon comprising solid material and at least one inlet for receiving processed gas from a sixth reactor, at least one discharge end, said at least one discharge end comprises at least one outlet connected with said at least one inlet for receiving processed carbon comprising solid material for reintroducing processed solid materials into said first fluid bed reactor and at least one outlet for gas, said fifth fluid bed reactor is operated at a temperature of 700° C. to 850° C., preferably 725° C. to 775° C., a hydrogen pressure of 200 to 300 mbar, preferably 225 to 275 mbar and an oxygen pressure of 10⁻⁵to 10⁻⁹mbar, preferably 10⁻⁶to 10⁻⁸;
  and
- f) a sixth reactor connected to at least one outlet for non-condensed gas for gasification of non-condensed gas from said third reactor, said sixth reactor comprises at least one intake, said at least one intake comprises at least inlet for receiving said non-condensed gas and at least one discharge end, said at least one discharge end comprises at least one outlet for transporting processed gas to said at least one inlet for receiving processed gas, said sixth reactor is operated at a temperature of 1100° C. to 1300° C., preferably 1150° C. to 1250° C., a hydrogen pressure of 200 to 300 mbar, preferably 225 to 275 mbar and an oxygen pressure of 10⁻⁵to 10⁻⁹mbar, preferably 10⁻⁶to 10⁻⁸.

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 advantageous thermal efficacy and high conversion rates. Additionally, the use of several specific reactors enables the system to be built up in a flexible and cost effective way. Moreover the system may be embedded in a local (agricultural) infrastructure in order to provide a relatively small scale conversion plant.
Yet another advantage of the present system is that the gas produced, or synthesis gas, is practically tar free, thereby avoiding clogging in the various applications.
The present first fluid bed reactor for thermal cracking according to the present invention 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. In the past, fuels and heavy oils were heated under pressure in large drums until they cracked into smaller molecules. However, 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. Preferably, is the oil vapour produced by the reactor removed within 2 seconds, thereby avoiding secondary cracking reactions. Additionally, the fluid bed reactor may comprise a Lewis acid. Preferably the fluid bed reactor is heated by hot gas from said fourth moving bed reactor.
The present second vapour wash reactor may, in the present context, also be denoted as vapour washer. A vapour washer washes the (hot) effluent vapour and gas and/or may separate heavy oil fractions. Preferably the present vapour wash reactor is a packed washing column. Preferably the vapour wash reactor is cooled directly by circulating product oil.
The present third reactor may also be denoted as fractionation reactor, or fractionation column. 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 fractionates the product oil or combustible oil. One example of fractionation reactor type is a packed column. The present third reactor may be cooled directly by circulating product oil.
“Carbon comprising solid material” or “solid material” within the present context is a material which is solid after processing in the present first fluid bed reactor. An example of such material is char or charred materials.
The present fourth moving bed reactor as used in the present context may also be denoted as a saturation reactor. This reactor stabilizes carbon in the solid materials, which solid materials are preferably derived from said first fluid bed reactor. The advantage of such a stabilisation processing is for example that stabilized char cannot longer contribute to the formation of tar.
Present fifth fluid bed reactor as used in the present context may also be denoted as quenching reactor or chemical quench. Preferably the fifth fluid bed reactor has a double role: gasification of the stabilised carbon comprising solid material while cooling the gas derived from, preferably, said sixth reactor. One advantage of this counterflow is thermal efficacy.
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. Preferably the sixth reactor according to the present invention is a pipe reactor.
According to a preferred embodiment of the present invention, 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 discharging non-carbon based material.
The present dryer is preferably a fluid bed reactor. The temperature in the dryer is preferably between 80° C. to 120° C., more preferably between 90° C. to 110° c. Preferably the oxygen pressure within the dryer is between 10 to 40 mbar. One advantage of the present dryer is that more carbon based materials can be processed. Accordingly, the applicability of the present system is increased.
According to another preferred embodiment, 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 homogeniser is preferably a stirred tank reactor. The temperature in the homogeniser is preferably between 80° C. to 120° C., more preferably between 90° C. to 110° c. Preferably the oxygen pressure within the homogeniser is between 1 to 10 mbar. One advantage of the present homogeniser is that more carbon based materials can be processed or converted. For example, oil sludges or tar sand can be processed in the system according to the present invention.
According to a preferred embodiment, the fifth reactor is connected through at least one outlet for gas with a gasfilter. The present gasfilter comprises at least one inlet for receiving gas and at least one outlet for discharging combustible gas.
The present gasfilter is preferably a sediment filter, more preferably a bagfilter. The gasfilter may be used for the removal from dust from the gas. Preferably operating temperature is between 200° C. and 240° C. It is preferred that the hydrogen pressure of the gasfilter is 200 to 300 mbar, more preferably 225 to 275 and/or the oxygen pressure is 10⁻⁵to 10⁻⁹mbar, more preferably 10⁻⁶to 10⁻⁸mbar.
According to a preferred embodiment, transport of solid material between the reactors is effected by fluming. More preferably the fluming is effected by pressurised gas. Through the use of fluming, hot process streams can be readily transported between the separate reactors.
According to a preferred embodiment, the pressure in the reactors is higher than atmospheric pressure.
According to yet another preferred embodiment, 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.
The present oxygen membrane may also be denoted as an oxygen transport membrane. Usually, oxygen membranes exploit unique properties of mixed conducting ceramic materials, which transport both oxygen and electrons across a gas impermeable membrane. According to the present system, the oxygen membrane is used for the selective transfer of oxygen ions to the present sixth reactor. Preferably the oxygen membrane comprises hollow ceramic elements. The temperature in the oxygen membrane is preferably of 850° C. to 1000° C.
According to another preferred embodiment, the gas from the outlet for gas of the fifth fluid bed reactor is transported to the gasfilter through the fourth moving bed reactor and/or the first fluid bed reactor. One advantage of this preferred embodiment is the thermal efficacy which is obtained by the using the heat of the gas of the fifth fluid bed reactor.
According to yet another preferred embodiment, the present carbon based materials are selected from the group consisting of biomass, wood, forestry waste products, organic waste, agricultural waste products, plastics and tires, or any combination thereof.
Considering the advantages of the present system, the present invention, according to another aspect, relates to a method for the thermal conversion of carbon based materials.
More specifically, the present invention relates to a method for the thermal conversion of carbon based materials into combustible oil and/or gas comprising introducing carbon based materials into a system according to the present invention.
In a preferred embodiment of the method according to the invention, the residence time in the first fluid bed reactor is 30 to 90 minutes, the residence time in the second vapour wash reactor is 0.5 to 5 seconds, the 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, and/or the residence time in the sixth reactor is 1 to 5 seconds.
According to yet another aspect, the present invention relates to the use of the present system for thermal conversion of carbon based materials into combustible oil and/or gas.

FIGURES

FIG. 1: shows an example of a preferred system for the thermal conversion of carbon based materials into combustible oil and/or gas according to the present invention;

FIG. 2: shows a GCMS analysis of the combustible oil obtained with the system according to the present invention;

FIG. 3: shows a system for thermal cracking of a hydrocarbons comprising mass.

FIG. 4: shows a system for thermal cracking of a hydrocarbons comprising mass.

FIG. 5: shows a system for cracking a pyrolysable mass.

FIG. 6: shows a system for the treatment of biomass.

DETAILED DESCRIPTION OF THE FIGURES.

To the FIGS. 1 to 2 will be further referenced in the example below.
FIG. 3 shows a system for the thermal cracking of a hydrocarbons comprising mass, comprising:

- a first cracking device (2) for the thermal separation of a mass comprising hydrocarbons in at least a substantially gaseous fraction and a charred product flow, the first cracking device (2) comprising first heating means (8) for heating the mass,
- a distillation device (3) connected with the discharge of the cracking device for the separation of a substantially gaseous fraction originating from the cracking device (2) in at least a heavy liquid fraction and at least a light fraction, whereby at least one discharge of the distillation device (3) is connected with the inlet of the cracking device (2) for leading back at least a part of the heavy liquid fraction from the distillation device to the cracking device (2), said distillation device (3) comprising at least one discharge for discharging said at least one light fraction,
- 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,
- a first gasification device (5) connected with the discharge of the second cracking device for the gasification of at least a part of the heavy liquid fraction originating from the separation device (4) to a first gas fraction, said first gasification device (5) comprising third heating means,
- a second gasification device connected with the discharge of the first gasification device for the gasification of at least a part of the rest fraction formed in the second cracking device to a second gas fraction, using the first gas fraction, said second gasification device being provided with a discharge for discharging at least a part of the first gas fraction and at least a part of the second gas fraction.
  Forthcoming, at least one discharge of the distillation device (3) is adapted for discharging at least one light liquid fraction and at least one further discharge of the distillation device is equipped for discharging at least one gaseous fraction. Thereby the synthesis gas may be lead as a heating gas through coils firstly the saturator (4) and secondly the thermal cracking process (2), before the synthesis gas preheats the air for the gasifier (5).

Further, the discharge of the distillation device adapted for discharging at said least one gaseous fraction is connected with an inlet of the first gasification device.
Further, the distillation device (3) comprises third heating means for heating the product flow led in the distillation device.
Further, the first cracking device and the second cracking device are the same device (2).
Further, the system comprises an aerator connected to the inlet of the first gasification device for supplying air to the first gasification device.
Further, the discharge of the second gasification device is connected with a thermally conducting discharge pipe for discharging the first gas fraction and the second gas fraction.
Further, the thermal conducting discharge pipe extends through the first cracking device, the second cracking device and/or the aerator.
Further, the discharge of the second cracking device is connected with the inlet of the first cracking device for leading back to the first cracking device at least a part of the heavy liquid fraction originating from the second cracking device.
Further, the separation device and the second gasification device are the same device (4)
Further, the second gasification device is provided with means for causing the first gas fraction to flow through the rest fraction.
Further, the system is provided with administration means connected to a discharge of the first gasification device for the administration of the first gas fraction to the second gasification device, whereby the means of administration extend to the lower zone of the second gasification device.
Further, a discharge for at least a part of the first gas fraction and/or at least a part of the second gas fraction is arranged in a way such that the means of administration extend to the lowermost zone of the second gasification device.
Further, the system reflects a method for the thermal cracking of a mass comprising hydrocarbons. The process can be 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° C. The third part is the chemical quench (3), where the hot synthesis gas of the gasifier (2) is used for for the endothermic gasification of the char from the saturator (1). 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 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 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. In particular said system, comprises the steps of:

- A) leading a mass comprising hydrocarbons in the first cracking device,
- B) separating the mass in an at least substantially gaseous fraction and a charred product flow by means of heating of the mass in the cracking device,
- C) leading at least a part of the substantially gaseous fraction to a distillation device,
- D) separating by means of distillation of the substantially gaseous fraction in the distillation device in at least a heavy liquid fraction and at least a light fraction,
- E) removing from the distillation device at least a part of the light fraction,
- F) leading back from the distillation device to the first cracking device of at least a part of the heavy liquid fraction,
- G) leading the charred product flow to the second cracking device,
- H) separating in the second cracking device the charred product flow in at least a heavy liquid fraction and a rest fraction by means of heating of the charred product flow,
- I) leading at least a part of the heavy liquid fraction to the first gasification device,
- J) converting at least a part of the heavy liquid fraction in a gas fraction by means of heating of the heavy liquid fraction,
- K) leading at least a part of the first gas fraction to the second gasification device,
- L) heating the rest fraction in the second gasification device by bringing the rest fraction in contact with at least a part of the first gas fraction, whereby at least a part of the rest fraction will be converted in a second gas fraction, and
- M) discharging at least a part of the first gas fraction and at least a part of the second gas fraction.

Further heating the mass during step B) to a temperature of between 200° C. and 700° C., preferably between 300° C. and 600° C.
Further separating of the mass during step B) in a reducing atmosphere.
Further heating the mass during step H) to a temperature of between 500° C. and 800° C., preferably between 500° C. and 600° C.
Further pyrolysing the mass during step H) in a reducing atmosphere.
Further, performing step C) in a time interval of between 1 and 10 seconds after step B) is initially performed.
Further, the heavy liquid fraction has a condensation temperature between 150° C. and 600° C.
Further, the light fraction has a condensation temperature lower than 150° C.
Further, leading the first gas fraction during step L) through at least a part of the rest fraction.
Further, fluidizing at least a part of the rest fraction during step L) by the first gas fraction flowing through the rest fraction.
Further, heating the mass during step B) to a temperature of between 500° C. and 800° C., preferably between 550° C. and 650° C.
Further, performing step D) during a time frame of between 0 to 10 seconds, preferably between 0 to 1 second.
Further, the heavy liquid fraction having a condensation temperature of between 150° C. and 600° C.
Further, heating the heavy liquid fraction during step D) to a temperature of 1100° C. and 1500° C., preferably between 1200° C. and 1400° C.
Further, performing the gasification according to step L) at a temperature of between 500° C. and 900° C., preferably between 700° C. and 800° C.
Further, the gas fraction comprises at least one substance selected from the group comprising: hydrogen, carbon monoxide, carbon dioxide, and steam.
FIG. 4 shows a system for the thermal cracking of a hydrocarbons comprising mass, comprising:

- a separation device (1) 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 (4) for heating of mass,
- 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.

Further, 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.
Further, the separation device and the second gasification device are part of the same device.
Further, the second gasification device is provided with means for causing the first gaseous fraction to flow through the rest fraction.
Further, the system comprises administration means connected with the discharge of the first gasification 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.
Further, 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.
Further, the system of FIG. 5 reflects a method for the thermal cracking of a mass, comprising hydrocarbons, in particular using a system according to FIG. 5, 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 liquid 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.

Further, the second gasification device and the separation device form part of the same device.
Further, leading the first gaseous fraction during step F) through at least a part of the rest fraction.
Further, the fluidisation of at least a part of the rest fraction during step F) by the gaseous fraction.
Further, heating the mass during step B) to a temperature between 500° C. and 800° C., preferably between 550° C. and 650° C.
Further, performing step D) within a time frame of 0 to 10 seconds, preferably within 0 to 1 second.
Further, the condensation temperature of the heavy liquid, being between 150° C. and 600° C.
Further, 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.
Further, performing of the gasification according to step G) at a temperature between 500° C. and 900° C., preferably between 700° C. and 800° C.
Further, the gaseous fraction comprising at least one substance selected from the group comprising carbon monoxide, carbon dioxide, and steam.
FIG. 5 shows a system for cracking a pyrolysable mass, particularly hydrocarbons, comprising:

- a cracking device (1) for the thermal cracking of a pyrolysable mass,
- a distillation device (2) connected with a discharge of the cracking device (1) for the separation of a from the cracking device (1) 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 (2) is connected with the inlet of the cracking device for the leading back from the distillation device (2) to the cracking device (1)of at least one part of the heavy liquid fraction, and whereby the distillation device (2) comprises at least a second discharge for discharging at least one light fraction.

Further, at least one second discharge of the distillation device (2) is equipped for the discharge of at least one light liquid fraction and that at least one other second discharge of the distillation device (2) is equipped for the discharge of at least one gaseous fraction.
Further, the cracking device (1) comprises first heating means for the heating of the pyrolysable mass
Further, the distillation device (1) comprises heating means for the heating of the in the distillation lead product flow.
Further, the system comprises at least one closing device for closing the discharge of the cracking device from the inlet of the distillation device.
Further, the system comprises at least one second closing device for closing the discharge of the distillation device from the inlet of the cracking device.
Further, the figure reflects a method for cracking of a pyrolysable mass, particularly hydrocarbons, preferably using the device according to FIG. 6, comprising the following steps:
A) leading of a pyrolysable mass into a cracking device (1),
B) at least partial pyrolysing of the mass by means of heating the mass in the cracking device (1) 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 (2),
D) by means of distillation separating the product flow in the distillation unit (2) in at least one heavy liquid fraction and at least one light fraction,
E) removing from the distillation device (2) 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 (2) to the cracking device of.
Further, heating the pyrolysable mass to a temperature of between 200° C. and 700° C., preferably between 300° C. and 600° C.
Further, pyrolysing of the mass during step B) in a reducing atmosphere.
Further, submitting the mass during the pyrolysing to a reducing substance that is formed by at least one substance chosen from the group consisting of: hydrogen, carbon monoxide, and steam.
Further, performing step C) within a timeframe of 1-10 seconds after step B) initially is performed.
Further, a heavy liquid fraction having a condensation temperature that amounts between 150-600° C.
Further, the light fraction having a condensation temperature being less than 150° C.
Further, steps B), C), D) being repeated at least one time after step F) is performed.
Further, the thermal cracking is operated typically at 300 to 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 second, 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.
FIG. 6 shows a system for the treatment of biomass, comprising:

- at least one 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,
- at least one eductor connected with the second discharge of the gasification device for pumping at least one part of the rest fraction of the combustible material out of the gasification device, said eductor also being connected with the first discharge of the eductor for the leading of product gas through the eductor as a propellant for the purpose of pumping the rest fraction out of the gasification device.

Further, FIG. 7 reflects a method for treating combustible material, preferably by using the system according to claim 1, comprising the following steps:
A) leading of the combustible material though the gasification device,
B) converting the biomass by means of heating in the gasification device in a product gas and a rest fraction,
C) discharging at least a part of the formed product gas through the first discharge from the gasification device, and
D) removing the gasification device at least a part of the rest fraction through the second discharge from the gasification device using an eductor, at least a part of the removed product gas being led through the eductor as a propellant.
Further, the product gas comprises at least one of the following components: flue gas, methane, water vapor, nitrogen, carbon monoxide, hydrogen, and/or carbon dioxide.
Further, the pneumatic transport is realized by an educator as a system to transport coal, coal products, charred material and ashes from one reactor to another using synthesis gas or flue gas as a drive gas. With pneumatic transport bulk particles are driven through pipes by means of blowing a gas, in most cases air, through the pipes at high speed.
The drive gas is blown in to an educator placed in the middle of the pneumatic system, therefore creating a flow of drive gas in one direction. This flow of drive gas creates a lower pressure in the pipe section before the joint where the educator is placed. The lower pressure creates a flow of gas created by a pyrolysis or gasification process, carrying particles from one reactor to the other. Because drive gas is flue gas or synthesis gas, no (partial) combustion of the gas or particles take place.
The principles of the present invention will be further detailed in the following example showing a preferred embodiment of the present invention. In the example, reference is made to FIGS. 1-2.

EXAMPLE

FIG. 1 shows a first fluid bed reactor (1) for thermal cracking of sludges, liquids and/or solids comprising carbon. The carbon based materials in the first fluid bed reactor (1) are subjected to the conditions:


	Temperature	400° C.
	Hydrogen pressure	250 mbar
	Oxygen pressure	10⁻⁷mbar
	Residence time mass	60 min.
	Residence time vapour	1 sec.
	Heating	indirectly by heat from
		saturator

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:


	Temperature	200° C.
	Hydrogen pressure	250 mbar
	Oxygen pressure	10⁻⁷mbar
	Residence time vapour	1 sec.
	Cooling	directly by circulating oil

The second vapour wash reactor (2) produces washed vapour and gas which is transported (104) to a third reactor (3). The remaining solids and oil are transported (105) to the first fluid bed reactor (1).
The washed vapour and gas are in the third reactor (3) subjected to the conditions:


	Temperature	40° C.
	Hydrogen pressure	250 mbar
	Oxygen pressure	10⁻⁷mbar
	Residence time gas	2 sec.
	Cooling	directly by circulating
		product oil

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:


	Temperature	900° C.
	Residence time gas	1 sec.

The oxygen membrane (10) produces oxygenated gas which is transported (108) to a sixth reactor (6) for gasification.
The oxygenated gas is in the sixth reactor (6) subjected to the conditions:


	Temperature	1200° C.
	Hydrogen pressure	250 mbar
	Oxygen pressure	10⁻⁷mbar
	Residence time gas/vapour	2 sec.

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:


	Temperature	750° C.
	Hydrogen pressure	250 mbar
	Oxygen pressure	10⁻⁷mbar
	Residence time medium	100 min.
	Residence time gas/vapour	1 sec.
	Heating	directly by heat from gasifier

The fifth fluid bed reactor (5) produces cooled gas and gasified stabilized carbon comprising solid material. 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 cooled gas is in the gasfilter (9) subjected to the conditions:


	Temperature	220° C.
	Hydrogen pressure	250 mbar
	Oxygen pressure	10⁻⁷mbar
	Residence time gas	2 sec.

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 remaining carbon comprising solid materials are in the fourth moving bed reactor (4) subjected to the conditions:


	Temperature	600° C.
	Hydrogen pressure	250 mbar
	Oxygen pressure	10⁻⁷mbar
	Residence time medium	200 min.
	Residence time gas/vapour	25 sec.
	Heating	directly by saturation heat

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:


	Temperature	100° C.
	Hydrogen pressure	25 mbar
	Residence time	variable, until dried.

The dryer (7) produces dried solid carbon based materials which are transported (115) to the first fluid bed reactor (1) and remaining metals and minerals are discharged (116) from the system and collected.
The homogenizer (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:


	Temperature	100° C.
	Hydrogen pressure
	5 mbar
	Residence time	variable, until homogenized

The homogenizer (8) produces homogenized liquid carbon based materials which are transported (117) to the first fluid bed reactor (1).

Results

By importing a mass of 1000 kg, containing plastics (20%), wood (40%) and organic waste (40%) in the system, the following products were obtained.

1635 kg/h synthesis gas
256 kg/h combustible oil

The calorific value of the synthesis gas obtained by the system according to the example was 5.1 MJ/Nm³. Moreover, the gas was free of tar.
An analysis of the combustible oil obtained by the above system is shown in table 1 below.
Forthcoming, the combustible oil obtained in the above example has a good quality, as is further elucidated by FIG. 2 which shows a GCMS analysis of the combustible oil obtained.

TABLE 1

ANALYTICAL REPORT SR-1322504.01.A02

	grade	GASOIL
	reference no.	Project No: 30102014
	sample 001	biodiesel 30102014 monster 8 1/5/10
	sample 002	biodiesel 30102014 monster 9 1/5/10
	date received	10.05.2010

	001	002

Density at 15° C., kg/m³	841.9	841.8
(DIN 51757)
° Calorific value, gross, MJ/kg	45.395	45.385
(ASTM D 240)
Flash point, Pensky Martens closed cup, ° C.	77.0	75.0
(EN ISO 2719, procedure A)
Kinematic viscosity at 20° C., mm²/s	4.480	4.477
(DIN 51562.1)
Distillation at 760 mm pressure
(EN ISO 3405)
percent evaporated at 250° C.	31.9	30.6
percent evaporated at 350° C.	93.9	94.1
Cold filter plugging point, ° C.	−10	−9
(EN 116)
Cloud point, ° C.	−8	−8
(EN 23015)
Micro carbon residue (on 10% distillation residue),	0.59	0.57
% wt (EN ISO 10370)
Sulphur, % wt (EN ISO 14596)	0.015	0.015

Claims

1. System for the thermal conversion of carbon based materials into combustible oil and/or gas comprising:

a first fluid bed reactor for thermal cracking of carbon based materials, the first fluid bed reactor comprising at least one intake, the at least one intake comprising at least one inlet for receiving carbon based materials, at least one inlet for receiving processed solid materials, and at least one inlet for receiving solids and oil, at least one discharge end, the at least one discharge end comprising at least one outlet for carbon comprising solid material, at least one outlet for metals and minerals, and at least one outlet for effluent vapor and gas;

a second vapor wash reactor connected to the outlet for effluent vapor and gas for washing effluent vapor and gas from the first fluid bed reactor, the second vapor wash reactor comprising at least one intake, the at least one intake comprising at least one inlet for receiving the effluent vapor gas, and at least one discharge end, the at least one discharge end comprising at least one outlet for washed vapor and gas, and at least one outlet for solids and oil connected to the inlet for solids and oil of the first fluid bed reactor for reintroducing the solids and oil into the first fluid bed reactor;

a third reactor connected to the outlet for washed vapor and gas for fractioning of the vapor and gas, the third reactor comprising at least one intake, the at least one intake comprising at least one inlet for receiving the washed vapor and gas, at least one discharge end, the at least one discharge end comprising at least one outlet for combustible oil, and at least one outlet for non-condensed gas;

a fourth moving bed reactor connected to the at least one outlet for carbon comprising solid material for stabilizing carbon in the solid material through conversion of gaseous materials, the fourth moving bed reactor comprising at least one intake, the at least one intake comprises at least one inlet for receiving the carbon comprising solid material, and at least one discharge end, the at least one discharge end comprising at least one outlet for stabilized carbon comprising solid material;

a fifth fluid bed reactor connected to the at least one outlet for stabilized carbon comprising solid material, the fifth fluid bed reactor comprising at least one intake, the at least one intake comprising at least one inlet for receiving the stabilized carbon comprising solid material, and at least one inlet for receiving processed gas from a sixth reactor, at least one discharge end, the at least one discharge end comprising at least one outlet connected with the at least one inlet for receiving processed carbon comprising solid material for reintroducing processed solid materials into the first fluid bed reactor, and at least one outlet for gas; and

a sixth reactor connected to at least one outlet for non-condensed gas for gasification of non-condensed gas from the third reactor, the sixth reactor comprising at least one intake, the at least one intake comprising at least inlet for receiving the non-condensed gas, and at least one discharge end, the at least one discharge end comprising at least one outlet for transporting processed gas to the at least one inlet for receiving processed gas.

2. The system according to claim 1, wherein the first fluid bed reactor is connected through the at least one inlet for receiving the carbon based materials with a dryer, the dryer comprising 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 discharging non-carbon based material.

3. The system according to claim 1, wherein the first fluid bed reactor is connected through the at least one inlet for receiving the carbon based materials with a homogenizer, the homogenizer comprising at least one inlet for receiving liquid carbon based materials, and at least one outlet for transporting homogenized liquid carbon based materials into the first fluid bed reactor.

4. The system according to claim 1, wherein the fifth reactor is connected through the at least one outlet for gas with a gasfilter, the gasfilter comprising at least one inlet for receiving gas, and at least one outlet for discharging combustible gas.

5.-6. (canceled)

7. The system according to claim 1 further comprising an oxygen membrane between the third reactor and the sixth reactor for oxygenation and/or oxidation of the non-condensed gas.

8. The system according to claim 4, wherein the gas from the outlet for gas of the fifth fluid bed reactor is transported to the gasfilter through one or both the fourth moving bed reactor and the first fluid bed reactor.

9. The system according to claim 1, wherein the carbon based materials are selected from the group consisting of biomass, wood, forestry waste products, organic waste, agricultural waste products, plastics and tires.

10. Method for the thermal conversion of carbon based materials into combustible oil and/or gas comprising introducing carbon based materials into the system according to claim 1.

11. The method according to claim 10, wherein the residence time in the first fluid bed reactor is in the range of approximately 30 to 90 minutes, the residence time in the second vapor wash reactor is in the range of approximately 0.5 to 5 seconds, the residence time in the third reactor is in the range of approximately 1 to 5 seconds, the residence time in the fourth moving bed reactor is in the range of approximately 180 to 240 minutes, the residence time in the fifth fluid bed reactor is in the range of approximately 30 to 120 minutes, and the residence time in the sixth reactor is in the range of approximately 1 to 5 seconds.

12. (canceled)

13. The system of claim 1, wherein first fluid bed reactor operates in a temperature range of approximately 350° C. to 450° C., a hydrogen pressure range of approximately 200 to 300 mbar, and an oxygen pressure range of approximately 10⁻⁵to 10⁻⁹mbar;

the second vapor wash reactor operates in a temperature range of approximately 150° C. to 300° C., a hydrogen pressure range of approximately 200 to 300 mbar, and an oxygen pressure range of approximately 10⁻⁵to 10⁻⁹mbar;

the third reactor operates in a temperature range of approximately 30° C. to 80° C., a hydrogen pressure range of approximately 200 to 300 mbar, and an oxygen pressure range of approximately 10⁻⁵to 10⁻⁹mbar;

the fourth moving bed reactor operates in a temperature range of approximately 550° C. to 650° C., a hydrogen pressure range of approximately 200 to 300 mbar, and an oxygen pressure range of approximately 10⁻⁵to 10⁻⁹mbar;

the fifth fluid bed reactor operates in a temperature range of approximately 700° C. to 850° C., a hydrogen pressure range of approximately 200 to 300 mbar, and an oxygen pressure range of approximately 10⁻⁵to 10⁻⁹mbar;

the sixth reactor operates in a temperature range of approximately 1100° C. to 1300° C., a hydrogen pressure range of approximately 200 to 300 mbar, and an oxygen pressure range of approximately 10⁻²to 10⁻⁵mbar; and

wherein the carbon comprising solid material from the first fluid bed reactor is reintroduced into the first fluid bed after been processed in the fourth, fifth and sixth reactors.

14. Method for the thermal conversion of carbon based materials into combustible oil and/or gas comprising:

operating a first fluid bed reactor in a temperature range of approximately 350° C. to 450° C., a hydrogen pressure range of approximately 200 to 300 mbar, and an oxygen pressure range of approximately 10⁻⁵to 10⁻⁹mbar, the first fluid bed reactor for thermal cracking of carbon based materials, the first fluid bed reactor comprising at least one intake, the at least one intake comprising at least one inlet for receiving carbon based materials, at least one inlet for receiving processed solid materials, and at least one inlet for receiving solids and oil, at least one discharge end, the at least one discharge end comprising at least one outlet for carbon comprising solid material, at least one outlet for metals and minerals, and at least one outlet for effluent vapor and gas;

operating a second vapor wash reactor in a temperature range of approximately 150° C. to 300° C., a hydrogen pressure range of approximately 200 to 300 mbar, and an oxygen pressure range of approximately 10⁻⁵to 10⁻⁹mbar, the second vapor wash reactor connected to the outlet for effluent vapor and gas for washing effluent vapor and gas from the first fluid bed reactor, the second vapor wash reactor comprising at least one intake, the at least one intake comprising at least one inlet for receiving the effluent vapor gas, and at least one discharge end, the at least one discharge end comprising at least one outlet for washed vapor and gas, and at least one outlet for solids and oil connected to the inlet for solids and oil of the first fluid bed reactor for reintroducing the solids and oil into the first fluid bed reactor;

operating a third reactor in a temperature range of approximately 30° C. to 80° C., a hydrogen pressure range of approximately 200 to 300 mbar, and an oxygen pressure range of approximately 10⁻⁵to 10⁻⁹mbar, the third reactor connected to the outlet for washed vapor and gas for fractioning of the vapor and gas, the third reactor comprising at least one intake, the at least one intake comprising at least one inlet for receiving the washed vapor and gas, at least one discharge end, the at least one discharge end comprising at least one outlet for combustible oil, and at least one outlet for non-condensed gas;

operating a fourth moving bed reactor in a temperature range of approximately 550° C. to 650° C., a hydrogen pressure range of approximately 200 to 300 mbar, and an oxygen pressure range of approximately 10⁻⁵to 10⁻⁹mbar, the fourth moving bed reactor connected to the at least one outlet for carbon comprising solid material for stabilizing carbon in the solid material through conversion of gaseous materials, the fourth moving bed reactor comprising at least one intake, the at least one intake comprises at least one inlet for receiving said the carbon comprising solid material, and at least one discharge end, the at least one discharge end comprising at least one outlet for stabilized carbon comprising solid material;

operating a fifth fluid bed reactor in a temperature range of approximately 700° C. to 850° C., a hydrogen pressure range of approximately 200 to 300 mbar, and an oxygen pressure range of approximately 10⁻⁵to 10⁻⁹mbar, the fifth fluid bed reactor connected to the at least one outlet for stabilized carbon comprising solid material, the fifth fluid bed reactor comprising at least one intake, the at least one intake comprising at least one inlet for receiving the stabilized carbon comprising solid material, and at least one inlet for receiving processed gas from a sixth reactor, at least one discharge end, the at least one discharge end comprising at least one outlet connected with the at least one inlet for receiving processed carbon comprising solid material for reintroducing processed solid materials into the first fluid bed reactor, and at least one outlet for gas; and

operating a sixth reactor in a temperature range of approximately 1100° C. to 1300° C., a hydrogen pressure range of approximately 200 to 300 mbar, and an oxygen pressure range of approximately 10⁻²to 10⁻⁵mbar, the sixth reactor connected to at least one outlet for non-condensed gas for gasification of non-condensed gas from the third reactor, the sixth reactor comprising at least one intake, the at least one intake comprising at least inlet for receiving the non-condensed gas, and at least one discharge end, the at least one discharge end comprising at least one outlet for transporting processed gas to the at least one inlet for receiving processed gas.

15. The method according to claim 14 further comprising operating at least one reactor with a residence time according to the following:

if the first fluid bed reactor, a residence time in the range of approximately 30 to 90 minutes;

if the second vapor wash reactor, a residence time in the range of approximately 0.5 to 5 seconds;

if the third reactor, a residence time in the range of approximately 1 to 5 seconds;

if the fourth moving bed reactor, a residence time in the range of approximately 180 to 240 minutes;

if the fifth fluid bed reactor, a residence time in the range of approximately 30 to 120 minutes; or

if the sixth reactor, a residence time in the range of approximately 1 to 5 seconds.

16. The method according to claim 14 further comprising operating each reactor with a residence time according to the following:

the first fluid bed reactor, a residence time in the range of approximately 30 to 90 minutes;

the second vapor wash reactor, a residence time in the range of approximately 0.5 to 5 seconds;

the third reactor, a residence time in the range of approximately 1 to 5 seconds;

the fourth moving bed reactor, a residence time in the range of approximately 180 to 240 minutes;

the fifth fluid bed reactor, a residence time in the range of approximately 30 to 120 minutes; and

the sixth reactor, a residence time in the range of approximately 1 to 5 seconds.

17. The method according to claim 14 further comprising homogenizing liquid carbon based materials, wherein the first fluid bed reactor is connected through the at least one inlet for receiving the carbon based materials with a homogenizer, the homogenizer comprising at least one inlet for receiving liquid carbon based materials, and at least one outlet for transporting the homogenized liquid carbon based materials into the first fluid bed reactor.

18. The method according to claim 14 further comprising transporting solid material between one or more of the reactors by fluming.

19. The method according to claim 14 further comprising operating one or more of the reactors at a pressure higher than atmospheric pressure.

20. The method according to claim 14 further comprising:

drying solid carbon based materials; and

introducing the dried solid carbon based materials into the first fluid bed reactor;

wherein the first fluid bed reactor is connected through the at least one inlet for receiving the carbon based materials with a dryer, the dryer comprising at least one inlet for receiving solid carbon based materials, at least one outlet for transporting the dried solid carbon based materials into the first fluid bed reactor, and at least one outlet for discharging non-carbon based material.

21. The method according to claim 14 further comprising discharging combustible gas, wherein the fifth reactor is connected through the at least one outlet for gas with a gasfilter, the gasfilter comprising at least one inlet for receiving gas, and at least one outlet for discharging the combustible gas.

22. The method according to claim 14 further comprising oxygenation and/or oxidation of non-condensed gas, wherein an oxygen membrane is provided between the third reactor and the sixth reactor for the oxygenation and/or oxidation of the non-condensed gas.

23. The method according to claim 14, wherein the carbon based materials are selected from the group consisting of biomass, wood, forestry waste products, organic waste, agricultural waste products, plastics and tires.

24. Method for the thermal conversion of carbon based materials into combustible oil and/or gas, wherein

the carbon based materials are thermally cracked in a first fluid bed reactor, to yield effluent vapor and gas and carbon comprising solid material;

the effluent vapor and gas are washed to yield washed vapor and gas, and solids and oil, said solids and oil being reintroduced into the first fluid bed reactor;

the washed vapor and gas are fractionated to yield non-condensed gas and a combustible oil;

the carbon comprising solid material is passed to a moving bed reactor, operated at a temperature of 550° C. to 650° C. to yield stabilized carbon comprising solid material;

the non-condensed gas is gasified to yield processed gas; and

the stabilized carbon comprising solid material and processed gas is passed to a fifth fluid bed reactor to gasify the stabilized carbon comprising solid material yielding gas and carbon comprising solid material; and

the carbon comprising solid material is reintroduced into said first fluid bed reactor.