(12) Oversettelse av europeisk patentskrift

Transkript

1 NO/EP (12) Oversettelse av europeisk patentskrift (11) NO/EP B1 (19) NO NORGE (1) Int Cl. F23C / (06.01) Patentstyret (21) Oversettelse publisert (80) Dato for Den Europeiske Patentmyndighets publisering av det meddelte patentet (86) Europeisk søknadsnr (86) Europeisk innleveringsdag (87) Den europeiske søknadens Publiseringsdato () Prioritet.02.16, FR, 14 (84) Utpekte stater AL AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO RS SE SI SK SM TR (73) Innehaver Morin, Jean-Xavier, 39 rue du Cas Rouge Marchandon, 4170 Neuville Aux Bois, FR-Frankrike (72) Oppfinner Morin, Jean-Xavier, 39 rue du Cas Rouge Marchandon, 4170 Neuville Aux Bois, FR-Frankrike (74) Fullmektig Tandbergs Patentkontor AS, Postboks 70 Vika, 0118 OSLO, Norge (4) Benevnelse DEVICE INTENDED IN PARTICULAR FOR THERMO-CHEMICAL CONVERSION (6) Anførte publikasjoner EP-A US-A US-A

2 1 EP NO/EP DEVICE INTENDED IN PARTICULAR FOR THERMO-CHEMICAL CONVERSION The invention relates to a compact device designed in particular for a thermochemical conversion in a continuous solid circulation loop. In order to capture, then store the carbon dioxide emissions from energy production installations using solid fuels of fossil or non-fossil origin, such as biomasses, technological developments have led to multiple channels that in particular aim to eliminate nitrogen from the air upstream from the installation by using oxygen produced by a cryogenic air separator unit, for example for the pre-capture of carbon dioxide by prior gasification of the fuels or for oxycombustion with quasi-pure oxygen mixed with recycled carbon dioxide and steam fumes. The oxygen production is the technological and economic constraint for these channels, which may be bypassed via the direct integration of the oxygen production into the combustion process by thermochemical conversion. Oxygen transport thermochemical conversions using metal oxides to produce pure carbon dioxide from fossil fuels date back to the 190s and used dense, interconnected fluidized beds. Then the use of the same techniques appeared for a different purpose, i.e., the combustion of fossil fuels for electricity production with integrated carbon dioxide capture, using circulating fluidized beds and instead of dense fluidized beds. The circulating solids are oxygen carrier solids. Thermochemical conversions via steam or flash pyrolysis gasification of reactive fuels such as biomasses, bituminous shales or bituminous sands intended to produce synthesis fuels or natural synthesis gas also use interconnected fluidized bed reactors, of the circulating fluidized bed and dense fluidized bed type. The circling solids are then inert solids such as sands, clays or alumina, or solids acting as catalysts or tar crackers, for example olivine, in order to reduce the tar content in the produced gases. Next, it appeared that the use of rapid fluidized beds and no longer of circulating fluidized beds alone is suitable for providing the flow rates of oxygen-carrier solid particles in order to ensure complete combustion and not partial oxidation of the fuels. The configuration generally adopted for thermochemical conversions of the combustion, gasification, pyrolysis type is that of two interconnected circulating fluidized bed loops for the circulation of circulating solid particles with, for each of the loops, a siphon and optionally a

3 2 EP NO/EP sulfur and carbon barrier. Such an installation has a certain complexity and increases the investment and maintenance costs. In the context of the worldwide deployment of this thermochemical conversion technology, in order to be able to meet low-power needs for industrial use under 0 MW, in particular in emerging countries, it is important to simplify the configuration and construction considerably in order to decrease costs and performance time frames. Furthermore, in a context of pressurization of thermochemical conversions to adapt them to downstream treatment and usage methods for the gases, for example a gas turbine, or in the context of industrial hydrogen production, it is important to simplify the configuration and construction as much as possible in order to reduce the overall bulk. Lastly, the direct coking between and 800 C of the bituminous sands using the dry method and the direct coking of bituminous shales, technique which makes it possible to separate the oils and the solid substrate, requires placing those fuels to be converted in contact with recycled solids performing a heat conductor role, at ratios between the recycled solids and the fuels to be converted of 3 to 40, which have never been achieved industrially to date. Document US 09/ A1 shows a device according to the preamble of claim 1. Patent document WO 09/02128 describes a fluidized bed reactor system including two circulating fluidized bed reactors and a particle line including a particle separator connected to the first reactor and equipped with a transport pipe for the particles of the first reactor to the second reactor. The second reactor is also equipped with a particle separator provided with a return pipe toward the second reactor. These two pipes have a cross-section substantially equal to the outlet cross-section of cyclone separators, and therefore a cross-section much smaller than that of cyclone separators or reactors. The manufacture of such a system therefore requires the use, management and storage of many sheets with different cross-sections, which makes it relatively cumbersome, complex and expensive to manufacture. The aim of the invention is to seek maximum compactness of such a system, preferably with thermochemical conversion, and reduce the investment costs thereof, while making it capable of performing complete conversion functions for solid fuels of fossil or non-fossil origin in the case of combustion and in the case of partial oxidation.

4 3 EP NO/EP In particular, the invention relates to an extremely simplified and inexpensive technological configuration, capable of accepting fuels of any nature, e.g., liquid, gaseous, solid or paste. This in particular applies to agricultural, forest and marine biomasses, peat, bituminous coals, bituminous shales, bituminous sands, sub-bituminous coals and oil residues, gases from methanization, unavoidable gases resulting from very CO2-rich oil in and gas exploitation, and lastly, solid urban waste and sludge. These units must allow the intensive circulation of solids, such as inert solids or oxygen-carrier oxides, their separation with gases, the control of the residence time of the solids in the reactors, and lastly, the tightness of the gas passages between two reactors to minimize parasitic gas intake between the two reactors. To that end, the invention proposes a rapid fluidized bed reactor including a lower base plate, a first associated separator and a transfer pipe for transferring solids leaving that separator, said pipe including a first siphon sealing against gases, the device being characterized in that said transfer pipe has a cross-section substantially equal to that of the associated reactor and the maximum cross-section of the associated separator. According to one preferred embodiment, the device comprises a first rapid fluidized bed reactor including a lower base plate, a first associated separator and a transfer pipe for transferring solids leaving that separator to a second reactor including a lower base plate, that pipe including a first siphon sealing against gases, a first outlet riser of which emerges in said second reactor, said second reactor being connected to a second associated separator connected to a second particle transfer pipe including a second siphon sealing against gases including a second outlet riser, and is characterized in that at least one of said transfer pipes has a cross-section substantially equal to that of the associated reactor and the maximum cross-section of the associated separator. Thus, it is not necessary to have a single type of sheath for each reactor and its associated transfer pipe. The invention thus proposes a simplified rapid fluidized bed configuration installation that combines two integrated reactors in series to perform a thermochemical conversion of the fuel combustion or gasification type with carbon dioxide capture. The invention also relates to the use of this device to form a thermochemical conversion installation.

5 4 EP NO/EP In that case, preferably, the first reactor is a rapid fluidized bed oxidation reactor, containing solid thermochemical reaction particles, and said second reactor is a combustion and rapid fluidized bed reduction reactor. The invention lastly relates to the use of that device to form a bituminous sand and/or sand treatment installation. In that case, preferably, the first reactor is a pyrolysis and cracking reactor for the bituminous sands and/or shales and the second reactor is a combustion reactor for the separated coke. The invention is described below in more detail using figures only showing preferred embodiments of the invention. Figure 1 is a diagrammatic elevation view of the device according to a first embodiment of the invention. Figure 2 is a developed diagrammatic view of a device according to a second embodiment of the invention. Figure 3 is a horizontal sectional view of the device according to the second embodiment of the invention, along plane III-III of figure 2. Figures 4 and are developed diagrammatic views of the device according to a third embodiment of the invention. As shown in figure 1, a device according to the invention comprises a first rapid fluidized bed reactor 1A with a constant cross-section and including a lower base plate 1E, a first associated separator 1B, preferably a cyclone separator with a side entrance inclined downward by an angle of to 3 relative to a horizontal plane, and a solids transfer pipe 1C at the outlet of that cyclone separator toward the bottom of the second reactor 2A with a constant cross-section and including a lower base plate 2E, that pipe 1C including a first gastight siphon 1D whereof a first outlet riser 1F emerges in the bottom of said second reactor 2A. The second reactor 2A is connected to a second associated separator 2B, preferably a cyclone separator with a side inlet inclined downward by an angle of to 3 relative to a horizontal plane, connected to a second particle transfer pipe 2C including a second gastight siphon 2D including a second outlet riser 2F. According to the invention, at least one of the transfer pipes 1C, 2C has a cross-section substantially equal to that of the associated reactor 1A, 2A and the maximum cross-section of the

6 EP NO/EP associated separator 1B, 2B. Preferably, as illustrated, two transfer pipes 1C, 2C have a crosssection substantially equal to that of the associated reactor 1A, 2A and the maximum crosssection of the associated separator 1B, 2B. The transfer pipes 1C, 2C are coaxial with the body of the corresponding cyclone 1B, 2B that respectively overhangs them. They are separated therefrom by an inwardly conical element or a simply conical element 6 that forms the inner space of the corresponding cyclone separator, which ensures complete integration and extremely simple construction, since all of the components have a cylindrical axis with a same section and can be built from the same raw component. The connection of the top of the circular fluidized bed reactors 1A, 2A and the associated cyclone separator 1B, 2B is done by a downwardly inclined pipe segment, the incline being comprised between and 3 relative to a horizontal plane. This 3 incline can be reduced if this segment has auxiliary fluidizations. Thus, a flow is obtained with the dense phase at the bottom of that pipe segment and a gravitational mass flow of solids is favored, which contributes to an optimal gas/solid separation performance in the cyclone separator. If one considers that the transfer pipes 1C, 2C have a circular section, the vertical height of the cyclone separators 1B, 2B is preferably comprised between 0. and times the diameter of the pipes, the incline angle of the wall of the lower cone is preferably comprised between and 2 degrees relative to a vertical plane, the diameter of the lower outlet of the separators, ensuring the gravitational discharge of the solids, is preferably comprised between 0.0 and 0. times the diameter of the pipes, the diameter of the upper outlet skirt 1G, 2G of the separators, ensuring the exit of the gases and fine solids, is preferably comprised between 0.2 and 0.6 times the inner diameter of the pipes, and the height of those outlet skirts is preferably 0.1 to times the height of the lateral inlet of the separators. The risers 1F and 2F preferably have a height rising from the bottom of the siphons 1D and 2D preferably comprised between 0. and times the diameter of the corresponding siphon 1D and 2D and a return angle toward the corresponding reactor 1A and 2A comprised between 3 and 70 degrees, optionally with an intermediate vertical segment depending on the needs of the arrangement of the reactors. Preferably, the siphons 1D, 2D also have a section identical to that of the reactors 1A, 2A.

7 6 EP NO/EP At least one of the transfer pipes 1C, 2C is vertical, and preferably, as illustrated, both transfer pipes 1C, 2C are vertical. The cyclone separators 1B, 2B have a vertical gas outlet 1G, 2G. Alternatively, the transfer pipes 1C, 2C may be slightly inclined by an angle smaller than or equal to relative to a vertical plane. At least one of the siphons 1D, 2D has a lower bottom 1H, 2H positioned in the same plane as the lower base plate 1E, 2E of the associated reactor, and preferably, as illustrated, both siphons 1D, 2D have a lower bottom 1H, 2H positioned in the same plane as the lower base plate 1E, 2E of the associated reactor. The second particle transfer pipe 2C is designed to transfer the particles from the second reactor 2A toward the bottom of the first reactor 1A. One preferred embodiment of this transfer will be described later. According to one preferred application of the invention, such a device is designed to form a thermochemical conversion installation. More specifically, the first reactor 1A is a rapid fluidized bed oxidation reactor, fluidized by air, containing solid thermochemical reaction particles, for example iron-, nickel-, titanium-, copper-based metal oxides and/or perovskites, preferably metal oxides, and the second reactor 2A is a combustion and rapid fluidized bed production reactor, fluidized by carbon dioxide mixed with steam. At the gas outlet of the first cyclone 1B, oxygen-depleted air is recovered and transmitted to a cooling device, a filtration device and a device for discharging it into the atmosphere. The first and second siphons 1D, 2D are fluidized by steam optionally mixed with recycled carbon dioxide. Thus, the reactor 2A is isolated from the fluidized bed reactor 1A upstream and downstream, regarding the gas. When the fuel is solid, the fuel is supplied by gravitational drop at the apex of the siphon 1D supplying the reactor 2A, by means of the feed 3, as illustrated in figure 1. When the fuel is liquid or gas, it is supplied directly in the rapid fluidized bed reactor 2A by injections, optionally mixed with carbon dioxide and steam. When the fuel is in paste form or in suspension, it is introduced by pumping and owing to injections distributed in the second rapid fluidized bed reactor 2A.

8 7 EP NO/EP When the installation is designed for a combustion, as shown in figure 1, the gas outlet of the second cyclone 2B made up of the conversion gas generated in the second reactor 2A between the metal oxides and the introduced fuel, and in particular containing carbon dioxide resulting from the conversion, is connected to a cooling device, a filtration device and a condensation device, for the transport and storage of the carbon dioxide. When the installation is intended for gasification or partial combustion, the gas outlet of the second cyclone 2B made up of the conversion gas generated in the second reactor 2A between the metal oxides and the introduced fuel in particular containing carbon dioxide, carbon monoxide, hydrogen, resulting from the conversion, is connected to a cooling device, a device for trapping alkalis of the NA 2 O and K 2 O type toward 600 C and a device for trapping tars around 400 to 800 C, preferably around 400 C, for use as feed gas for the motor or after prior compression in a gas turbine or directly into feed gas for the burners of an existing or new boiler. The thermochemical conversions by steam gasification or flash pyrolysis of reactive fuels such as biomasses, bituminous shales or bituminous sands such as biomasses, designed to produce synthesis fuels or natural synthesis gas, may also use the device according to the invention. The circulating solids are then inert solids such as sands, clays or alumina, or solids of the olivine type acting as catalysts in order to reduce the tar content in the produced gases. The direct coking between and 800 C of the bituminous sands using a dry method and direct coking of the bituminous shales, technique which makes it possible to separate oils and the solid substrate, requires placing those fuels to be converted in contact with recycled solids performing a heat conduction role, at ratios between the recycled solids and the fuels to be converted of 3 to 40, which have never been achieved industrially to date. The device according to the invention may also be used, the circulating solids then being inert solids such as sands or minerals contained in the fuels to be converted. Figures 2 and 3 illustrate a second embodiment of the invention that ensures particularly significant compactness of the device that may also be used for all of the applications already specified above, among others. The two transfer pipes 1C, 2C are vertical and the two outlet risers 1F, 2F are vertical, and the vertical central axis of the first reactor 1A, the vertical central axis of the first associated separator 1B and the first transfer pipe 1C, the vertical central axis of the first outlet riser 1F, the vertical central axis of the second reactor 2A, the vertical central axis of the second associated

9 8 EP NO/EP separator 2B and the second transfer pipe 2C, and the vertical central axis of the second outlet riser 2F are the apices of a hexagon, preferably regular, as shown in figure 3. The device then includes a central pylon 4 for the mechanical support of the first reactor 1A, the first associated separator 1B, the first outlet riser 1F, the second reactor 2A, the second associated separator 2B and the second outlet riser 2F. Preferably, for small units, the pylon 4 includes a central cooling tube 4A and at least one outer enclosure connected to the gas outlet of at least one of said separators. Preferably, as illustrated, it includes two outer enclosures 4B, 4C respectively connected to the gas outlet of the first separator 1B and the second separator 2B. In the context of a pressurized enclosure, this arrangement greatly simplifies the overall mechanical design and makes it possible to accommodate the heat expansion of the enclosures. In place of this type of pylon, depending on the size of the unit, vertical cooling exchangers for the gases coming from the cyclone separators 1B, 2B are positioned above the risers 1F, 2F of the siphons and fit in the hexagonal pitch of the components. In these first embodiments, the height of the reactors 1A, 2A is the same. It may be necessary for them to have different heights, since the reactions involved in each of the reactors may have very different kinetics, for example rapid oxidation and slow reduction of the oxygencarrier solids, or slow conversion of fuels during the reduction. Figure 4 shows a third embodiment, where the reactors 1A, 2A have different heights. As shown in this figure, a device according to the invention, which preferably is also installed in a hexagonal loop as previously described, comprises a first rapid fluidized bed reactor 1'A with a constant cross-section and including a lower base plate 1'E, a first associated separator 1'B, preferably a cyclone separator with an inlet side downwardly inclined by an angle of to 3 relative to the horizontal plane, and a solid transfer pipe 1'C at the outlet of that second separator toward the bottom of the second reactor 2'A with a constant cross-section including a lower base plate 2'E, that pipe 1'C including a first gastight siphon 1'D, whereof a first outlet riser 1'F emerges in the bottom of said second reactor 2'A. The second reactor 2'A is connected to a second associated separator 2'B, preferably a cyclone separator with a side inlet inclined downwardly by an angle from to 3 relative to a horizontal plane, connected to a second particle transfer pipe 2'C including a second gastight siphon 2 D including a second outlet riser 2'F.

10 9 EP NO/EP According to the invention, at least one of the transfer pipes 1 C, 2 C has a cross-section substantially equal to that of the associated reactor 1 A, 2 A and the maximum cross-section of the associated separator 1 B, 2 B. Preferably, as illustrated, the two transfer pipes 1 C, 2 C have a cross-section substantially equal to that of the associated reactor 1 A, 2 A and the maximum cross-section of the associated separator 1 B, 2 B. Preferably, the siphons 1 D, 2 D also have a section identical to that of the reactors 1 A, 2 A. The transfer pipes 1 C, 2 C are coaxial with respect to the body of the corresponding cyclone 1 B, 2 B, which respectively overhangs them. They are separated therefrom by an inwardly conical element that forms the inner space of the corresponding cyclone separator, which ensures total integration and extremely simple construction, since all of the components have a cylindrical axis with a same section and can be built from the same raw component. According to this embodiment, the first transfer pipe 1 C is therefore extended downstream from the first siphon 1 D of a second transfer pipe segment 1 C with a same section and that is also vertical, ensuring the transfer toward the bottom of the second reactor 2 A. According to the preferred application to a thermochemical loop, the bottom of the first reactor 1 A is supplied with fluidization gas GF and also includes an upper secondary fluidization level to act on the filling with solids of the lower zone of the reactor and act on their residence time. The same is true for the second reactor 2 A. Furthermore, one of the two reactors may have a solid recirculation loop on itself, so as to constitute an overall solid circulation arrangement in a loop and a half for circulation of solids, instead of only one. This has the advantage of being able to ensure long residence times of the solids in one of the two reactors. According to the illustrated example, it is the second reactor 2 A that has a recirculation loop on itself, using an additional riser 2 F installed on the second siphon 2 D. Furthermore, each siphon bottom 1 D, 2 D may constitute an additional reaction chamber, complementary to each reactor 1 A, 2 A so as to ensure the injection of reactive or inert gases, reactive or inert solids, to elutriate and/or attrite fine solids contained in the circulating bed. As illustrated in figure 4, these sides and bottoms are then supplied with fluidization gas GF and are equipped with a solids discharge ES. Preferably, the outlet gas SG of each separator 1 B, 2 B is recycled on each reactor 1 A, 2 A, to contribute to supplying its own fluidization, but also in a crossed manner with the

11 NO/EP EP opposite reactor to constitute arrangements of reactors in series on the side. One typical example such an application is indirect retorting (in French, a cracking or pyrolysis and evaporation assembly) of bituminous sands or shales, in which the combustion fumes of a reactor supply the fluidization of the other reactor that performs the retorting of the bituminous sands or shales. Radial cooling panels PR can equip the top of the reactors 1 A, 2 A as well as the outlet and recycling pipes for the outlet gases SG of the separators 1 B, 2 B. The first siphon 1 D includes a feed 3 of solids and/or bed supplement to be converted. Figure shows a device of the same type, applied to the treatment of bituminous sands or shales. In this application, the first reactor 1 A is a pyrolysis and cracking reactor, and the second reactor 2 A is a combustion reactor for the separated coke, supplied with sand or shales with coke deposited by the first transfer pipe 1 C, 1 C. The fluidization gas GF is combustion air. The feed 3 of bituminous sands or shales is provided at the second siphon 2 D. In that case, the bottom of the second siphon 2 D constitutes an additional reaction chamber, complementary to the second reactor 2 A. The bottom of that siphon is then supplied with fluidization gas GF and is equipped with a solids discharge ES, the solids being made up of the treated sand or shale. The hot fumes SG leaving the second separator 2 B are completely recycled on the first reactor 1 A, in order to ensure its fluidization, and radial cooling panels PR only equip the outlet pipe for the outgoing gases SG of the first separator 1 B made up of a separated oil products. The description above describes preferred embodiments, but the invention also covers alternatives of those embodiments. The section of the reactors and the other elements may be circular, square or rectangular, preferably with a ratio below 1. between the width and the length. The section of one of the reactors, and therefore its associated transfer pipe, may be different from the section of the other reactor, and therefore its associated transfer pipe, preferably with a ratio below 1.. As an example, the device according to the invention applies to any installation size, the diameter or width of the reactors being able to be comprised between 0.03 and meters, their height being able to be comprised between 0. and 2 meters and the reactors operating at an atmospheric pressure of bars.

12 1 EP NO/EP236976

13 2 EP NO/EP236976

14 3 EP NO/EP236976

15 4 EP NO/EP236976

16 NO/EP Patentkrav EP Anordning omfattende en hurtig virvelsjiktreaktor (1A, 1'A) som inkluderer en nedre basisplate (1E, 1'E), en første assosiert separator (1B, 1'B) og et overføringsrør (1C, 1'C) for overføring av faste stoffer som forlater separatoren (1B, 1'B), idet røret (1C, 1'C) som inkluderer en første vannlås (1D, 1'D) som tetter mot gasser, der anordningen er karakterisert ved at nevnte overføringsrør (1C, 1'C) har et tverrsnitt i det vesentlige lik det til den tilknyttede reaktor (1A, 1'A) og det maksimale tverrsnittet til den assosierte separator (1B, 1'B). 2. Anordning ifølge krav 1, omfattende en første hurtig virvelsjiktreaktor (1A, 1'A) som inkluderer en nedre basisplate (1E, 1'E), en første assosiert separator (1B, 1'B) og et overføringsrør (1C, 1'C) for å overføre faste stoffer som forlater separatoren (1B, 1'B) til en andre reaktor (2A, 2'A) som inkluderer en nedre bunnplate (2E, 2'E), idet røret (1C, 1'C) inkluderer en første vannlås (1D, 1'D) som tetter mot gasser, et første uttaksstigerør (1F, 1'F) som fremkommer i den nevnte andre reaktor (2A, 2'A), idet den andre reaktor er forbundet til en andre assosiert separator (2B, 2'B) som er forbundet med et andre partikkeloverføringsrør (2C, 2'C) som inkluderer en andre vannlås (2D, 2'D) som tetter mot gasser inkludert et andre utløpsstigerør (2F, 2'F), der anordningen er karakterisert ved at minst én av nevnte overføringsrør (1C, 1'C, 2C, 2'C) har et tverrsnitt i det vesentlige lik det til den assosierte reaktor (1A, 1'A, 2A, 2'A) og det maksimale tverrsnittet til den assosierte separator (1B, 1'B, 2B, 2'B). 3. Anordning ifølge foregående krav, karakterisert ved at minst ett av de nevnte overføringsrør (1C, 1'C, 2C, 2'C) er vertikale. 4. Anordning ifølge krav 2 eller 3, karakterisert ved at separatorene (1B, 1'B, 2B, 2'B) er syklonseparatorer som er koaksiale med det assosierte overføringsrøret, med et sideveis innløp som er nedad hellende med en vinkel på til 3 i forhold til et horisontalplan.. Anordning ifølge et av kravene 2 til 4, karakterisert ved at minst én av nevnte vannlåser (1D, 1'D, 2D) har en nedre bunn som er plassert i samme plan som den nedre basisplaten (1E, 1'E, 2E) til den assosierte reaktoren. 6. Anordning ifølge ett av kravene 2 til, karakterisert ved at det andre partikkeloverføringsrøret (2C, 2'C) er utformet for å overføre partikler fra nevnte andre reaktor (2A, 2'A) til nevnte første reaktor (1A, 1'A).

17 NO/EP Anordning ifølge ett av kravene 3 til 6, karakterisert ved at de to overføringsrørene (1C, 2C) er vertikale og de to uttaksstigerør (1F, 2F) er vertikale, og ved at den vertikale midtakse til nevnte første reaktor (1A), den vertikale midtakse til den første assosierte separator (1B), den vertikale midtakse av nevnte første utløpsstigerør (1F), den vertikale midtakse til den andre reaktor (2A), den vertikale midtakse til nevnte andre assosierte separator (2B) og den vertikale midtakse til det andre utløpsstigerøret (2F) er spissene i et heksagon. 8. Anordning ifølge foregående krav, karakterisert ved at nevnte heksagon er regulært. 9. Anordning ifølge krav 7 eller 8, karakterisert ved at den omfatter en sentral mekanisk maststøtte (4) til den første reaktor (1A), nevnte første assosierte separator (1B), det første utløpsstigerøret (1 F), nevnte andre reaktor (2A), nevnte andre assosierte separator (2B), og det andre utløpsstigerøret (2F).. Anordning ifølge det foregående krav, karakterisert ved at masten (4) har et sentralt kjølerør (4A) og minst én ytre kapsling (4B, 4C) som er forbundet til gassutløpet ved minst én av nevnte separatorer (1B, 2B). 11. En termokjemisk konversjonsinstallasjon, som består av anordningen ifølge ett av kravene 2 til Installasjon ifølge krav 11, karakterisert ved at nevnte første reaktor (1A) er en hurtig virvelsjikt-oksidasjonsreaktor, som inneholder termoreaksjonspartikler i fast form, og der nevnte andre reaktor (2A) er en hurtig virvelsjikt-forbrennings- og reduksjonsreaktor. 13. Installasjon ifølge krav 12, karakterisert ved at nevnte første reaktor (1A) danner virvelsjikt av luft og nevnte andre reaktor (2A) danner virvelsjikt av karbondioksid. 14. Installasjon ifølge krav 13, karakterisert ved at nevnte første vannlås (1 D), og nevnte andre vannlås (2D) leveres med en blanding av damp og karbondioksid. 3. System ifølge et av kravene 12 til 14, karakterisert ved at nevnte første vannlås (1 D) inkluderer en drivstofftilførsel. 16. En installasjon for behandling av bituminøse sand og/eller leirskifer, som består av en anordning ifølge ett av kravene 2 til 11.

18 NO/EP Installasjon ifølge krav 16, karakterisert ved at den første reaktor (1'A) er en pyrolyse og spaltningsreaktor for bituminøs sand og/eller leirskifer og den andre reaktor (2'B) er en forbrenningsreaktor for den separerte koks. 18. Installasjon ifølge krav 17, karakterisert ved at nevnte første reaktor (1'A) danner virvelsjikt av gasser som forlot den andre reaktor, og den annen reaktoren (2'A) danner virvelsjikt av luft. 19. Installasjon ifølge krav 18, karakterisert ved at den første vannlås (1'D) og den andre vannlås (2'D) danner virvelsjikt av luft.. Installasjon ifølge et av kravene 16 til 19, karakterisert ved at andre vannlås (2'D) inkluderer en tilførsel av bituminøs sand og/eller leirskifer.