WO1994016807A1 - Appareil de traitement d'une boue solide/liquide et reacteur catalytique multi-phase - Google Patents

Appareil de traitement d'une boue solide/liquide et reacteur catalytique multi-phase Download PDF

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Publication number
WO1994016807A1
WO1994016807A1 PCT/NO1994/000023 NO9400023W WO9416807A1 WO 1994016807 A1 WO1994016807 A1 WO 1994016807A1 NO 9400023 W NO9400023 W NO 9400023W WO 9416807 A1 WO9416807 A1 WO 9416807A1
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WO
WIPO (PCT)
Prior art keywords
filtrate
slurry
zone
filter element
vessel
Prior art date
Application number
PCT/NO1994/000023
Other languages
English (en)
Inventor
Erling Rytter
Per Roterud
Petter Lian
Trond Myrstad
Original Assignee
Den Norske Stats Oljeselskap A.S.
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Den Norske Stats Oljeselskap A.S. filed Critical Den Norske Stats Oljeselskap A.S.
Priority to CA002154184A priority Critical patent/CA2154184C/fr
Priority to GB9515370A priority patent/GB2289856B/en
Priority to AU60119/94A priority patent/AU6011994A/en
Publication of WO1994016807A1 publication Critical patent/WO1994016807A1/fr
Priority to DK199500849A priority patent/DK172646B1/da
Priority to NO952956A priority patent/NO300799B1/no

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/005—Separating solid material from the gas/liquid stream
    • B01J8/006—Separating solid material from the gas/liquid stream by filtration
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/1836—Heating and cooling the reactor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/20—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium
    • B01J8/22—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium gas being introduced into the liquid
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2/00—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
    • C10G2/30—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen
    • C10G2/32—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts
    • C10G2/34—Apparatus, reactors
    • C10G2/342—Apparatus, reactors with moving solid catalysts
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00106—Controlling the temperature by indirect heat exchange
    • B01J2208/00115—Controlling the temperature by indirect heat exchange with heat exchange elements inside the bed of solid particles
    • B01J2208/00132—Tubes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00245—Avoiding undesirable reactions or side-effects
    • B01J2219/0025—Foam formation

Definitions

  • the present invention relates to a reactor for conducting a continuous multi-phase catalytic reaction and is particularly, though not exclusively, applicable to the catalytic conversion of syngas, produced by the reforming of methane, to hydrocarbon fuels, by a Fischer- Tropsch type of synthesis.
  • Other reaction systems for which the apparatus would be suitable include various slurry reactions for the production of petrochemicals, the production of oxygenates from synthesis gas and dehydrogenation reactions. Additionally, however, the apparatus is equally useful in solid/liquid slurry treatment applications.
  • Three-phase catalytic reaction systems are used in a number of chemical processes and their application in the petrochemical industry appears to be increasing.
  • mechanically agitated slurry reactors employ small catalyst particles dispersed in the liquid and so in most applications, the liquid will have to be separated from the slurry to remove liquid products or for catalyst regeneration purposes. In those cases where the liquid is an inert medium, occasionally, it may have to be replaced due to degradation or the build-up of impurities.
  • Mechanically agitated slurry reactors are particularly convenient for batch processes due to the low mass-transfer and heat resistance. These features also make them suitable for the determination of reaction kinetics in the laboratory.
  • a serious disadvantage and limitation of this reactor type is the difficulty in the separation of catalyst particles in any continuous operation.
  • solid/liquid slurry reaction apparatus for reactions in which a liquid product is formed in a slurry phase including a finely divided catalyst in a liquid medium
  • the apparatus comprising: a reaction vessel defining a reaction zone arranged to accommodate the slurry phase and a volume of gas above the slurry phase; means for introducing gaseous reactants and/or other components into the slurry phase in the lower region of the vessel; a filtration section arranged to separate the liquid product from the slurry phase, the filtration section including a housing and a filter element which together define a filtrate zone, the filtrate zone having an outlet for the product filtrate; means establishing fluid communication between the filtrate zone and that part of the reaction zone which in use is to be occupied by the volume of gas above the slurry phase; means for establishing a mean pressure differential across the filter element; in one embodiment, the means for establishing a mean pressure differential across the filter element comprises a valve and a control unit connected to the outlet of the filtrate zone
  • the apparatus may also be used for slightly different purposes, such as treatments of various kinds, e.g., ion exchange, purifica ions, removal of unwanted components (traces of impurities, discolourations) .
  • treatments of various kinds e.g., ion exchange, purifica ions, removal of unwanted components (traces of impurities, discolourations) .
  • the present invention provides a solid/liquid slurry treatment apparatus in which a liquid product is separated from a slurry phase containing finely divided catalyst in a liquid medium, the apparatus comprising: a vessel defining a treatment zone arranged to accommodate the slurry phase and a volume of gas above the slurry phase; means for introducing gaseous reactants and/or other components into the slurry phase in the lower region of the vessel; a filtration section arranged to separate the liquid product from the slurry phase, the filtration section including a housing and a filter element which together define a filtrate zone, the filtrate zone having an outlet for the product filtrate; means establishing fluid communication between the filtrate zone and that part of the treatment zone which in use is to be occupied by the volume of gas above the slurry phase; means for establishing a mean pressure differential across the filter element; and in which the filter element is arranged to be in contact with the slurry in the slurry zone and the housing at least partially surrounds the vessel.
  • reaction zone will be used to refer to the reaction zone or the treatment zone, as appropriate.
  • This is believed to be achieved as follows.
  • the turbulent motion of the slurry, as gas bubbles pass up through it, causes fluctuations or oscillations in pressure at the filter element.
  • the fluid communication between the reaction zone and the filtrate zone facilitates or enhances these pressure fluctuations or oscillations.
  • the housing circumferentially surrounds the reactor vessel for at least a portion of the extent of the reactor vessel.
  • the filter element may be provided by a portion of the wall of the reactor vessel which is composed of a filter material.
  • the filter element is located outside the vessel and the vessel is discontinuous in the region of the filter element.
  • the filter element is located within the vessel and the housing is constituted by a portion of the vessel wall.
  • the fluid communication is between the volume of gas above the slurry phase and a volume of gas above the filtrate.
  • the pressure differential may result from the hydrostatic pressure arising from the slurry in the reaction vessel having a higher hydrostatic level than the filtrate in the filtrate zone.
  • the communication between the space above the slurry in the reaction zone and the space above the filtrate in the filtrate zone prevents the build up of pressure differentials in excess of that corresponding to the hydrostatic pressure.
  • the communication may conveniently be via a tube extending between the top of reaction zone and the top of the filtrate zone and being open to each.
  • the tube connecting the two volumes of gas is arranged to facilitate the escape of any gas accumulating in the upper portion of the filtrate zone.
  • the amplitude or magnitude of the fluctuations or oscillations in the pressure differential across the filter element is about the same magnitude or greater than the mean value of the static pressure differential.
  • the mean pressure differential across the filter element should be kept at a rather low level, typically less than 6 mBar (600Pa) . If the mean pressure differential is below a critical vale (6 mbar in case of the exemplified system) , the filter is self cleaning. With slightly higher values, build-up of a cake of particles on the filter surface will occur, as one would expect for a filter, and the capacity will gradually decrease. This cake will disappear if the flow through the system is reversed (backflushed) , and the original capacity will be regained.
  • the fluid communication tube may, in addition to effecting the communication between the gas phase above the slurry and the internal parts of the filtration section, also provide an easy escape route for gas which may have penetrated the filter element and which otherwise would have become entrapped in the filtrate zone. Gaseous products or components may be allowed to escape by any convenient means such as a separate outlet from the reaction vessel or simply via the fluid communication tube. Experiments carried out suggest that if the tube is closed or severely choked, the filter element would rapidly become clogged. Of course, the fluid communication tube will set a limit to the pressure drop across the filter element and thus as stated, prevent unwanted and damaging pressure build-ups, which might well otherwise occur when there is a considerable pressure drop between internal parts of the reaction vessel and the outlet side.
  • the filter element comprises a fine meshed screen, helically wound threads, fine vertical threads or sintered metal particles.
  • the surface of the filter element which is in contact with the slurry is rendered smooth.
  • the filter element material and catalyst are preferably selected so that the maximum hole or pore size in the filter element is of the same order of magnitude as the catalyst particle size.
  • the particle size is preferably not less than half the pore size.
  • the means for introducing gaseous reactants or components may comprise any suitable means such as a bubble cap plate, a plurality of nozzles, a frit plate, etc, preferably located at the bottom of the reaction vessel.
  • the reactants may be CO and H 2 , for example from the reforming of natural gases, and the products may be methanol and higher hydrocarbons.
  • the pressure fluctuation value may be of the order of the pressure differential, for example from 10 to 200% of the pressure differential.
  • the actual value of the pressure differential may be from 1 to 100 mBar, preferably 2 to 50 mBar.
  • the vessel is preferably provided with an inlet and/or an outlet for liquid reactants or components and preferably also an outlet for gas in its upper part.
  • the apparatus may also include means for flushing the filtration section and the filter elements.
  • the outlet from the filtrate zone is arranged to provide a constant level for the filtrate in the filtrate zone.
  • the outlet from the filtrate zone comprises an inverted U-shaped pipe whose top section defines the liquid level in the filtrate zone.
  • the outlet from the filtrate zone includes a weir within the filtration section which defines the liquid level in the filtrate zone.
  • the outlet from the filtrate zone comprises an upwardly extending pipe within the filtrate zone which is open at a level which defines the liquid level in the filtrate zone.
  • the reaction vessel is provided with means for heat transfer.
  • This may comprise a plurality of vertically positioned tubes intended for circulation of a heat transfer medium.
  • the fluid communication between the gas spaces above the slurry and filtrate zones is by means of a communication tube.
  • the wall of the reaction vessel terminates and the filtration section housing forms a dome over the top of the reaction vessel whereby the volume of gas above the slurry and the volume of gas above the filtrate are in direct communication.
  • a higher effective filter area may be provided. This may be achieved by adopting a more intricate or complex filter element profile.
  • the filtration sections include vertically spaced filter elements and housings which may or may not partly overlap. In an alternative embodiment however there may be plurality of vertically spaced filtration sections.
  • the respective filtration section housings are in the form of flanged pipe section which are screwed e.g. bolted together to form a rigid structure.
  • the invention is particularly well adapted for use in a method of converting natural gas (methane) to higher hydrocarbon fuels which involves initially converting the natural gas into synthesis gas, either by steam reforming, partial oxidation, a combination of the two, or otherwise reforming the methane to produce carbon monoxide and hydrogen, subjecting the CO and H 2 to catalytic conversion by a Fischer-Tropsch synthesis to form higher hydrocarbon fuels such as liquid paraffin waxes, and subsequently separating and/or cracking these products to produce the required range of hydrocarbons.
  • FIGS. 2 and 3 are simplified schematic sections through a part of the filtration section showing two alternative systems for achieving a constant filtrate level
  • Figure 4 is a view similar to Figures 2 and 3 showing an alternative location for the filter elements
  • Figure 5 is a partial perspective sketch of part of the filtration section showing another possible location for the filter element
  • Figure 6 is a schematic horizontal cross-section showing an alternative filter arrangement
  • Figure 7 is a simplified view similar to Figure 1 showing an alternative embodiment
  • Figure 8 is an enlarged vertical cross-section of the filtration system of a further embodiment
  • Figure 9 is a partial vertical cross-section of a still further embodiment; and Figure 10 is a graph showing the results of an experimental example.
  • the reaction apparatus 11 includes a reactor vessel 12 and a filtration section 13.
  • the reactor vessel 12 includes a generally tubular section 14 and above this, an inverted cone-shaped portion 15.
  • the tubular section 14 defines the slurry zone 20 in which a slurry of finely divided catalyst in a liquid medium of eg product hydrocarbon is accommodated.
  • the cone-shaped portion 15 acts as an expansion chamber to prevent the slurry from foaming over and defines a gas space 16 above the reaction zone.
  • the cone-shaped portion 15 may contain additional means (not shown) for breaking up or reducing foam formation.
  • a series of heat transfer tubes 21 are located within the reactor vessel extending between a common inlet 22 and a common outlet 23 for a heat exchange medium.
  • the apparatus 11 will be controlled by a large number of transducers, controllers valves, pumps etc, one of which (a pressure or temperature sensor) is indicated by way of example at 24.
  • the filtration section 13 comprises an annular housing 25 which surrounds the vessel 12 just below the cone-shaped portion 15. Within the housing 25, a part of the vessel wall is composed of sintered metal and thus constitutes a filter element 26. Non-porous parts 27 of the vessel wall extend into the housing 25 at the top and bottom of the housing. The housing 25 and vessel wall effectively define a filtrate zone 28 and above it, a gas space 29. An outlet from the filtrate zone 28 serves as a constant level device for the filtrate.
  • a pipe 31 extends upwards from an outlet opening 32 near the bottom of the housing 25.
  • a horizontal connection section 33 defines the level 34 of the filtrate in the filtrate zone 28 and extends downwards to an outlet valve 35. The valve 35 is opened to empty the accumulated liquid product in the downward leg of the pipe. Of course, the downward leg may be replaced by a holding tank for the liquid product.
  • the outlet pipe 31 is filled with liquid product between the opening 32 and the horizontal section 33.
  • a communication tube or pipe 38 connects the two gas spaces 16 and 29.
  • the tube 38 has a valve 39.
  • the communication tube 30 is also connected to the pipe 31 thus providing fluid communication between the gas spaces 16, 29 and the outlet pipe 31.
  • the housing 25 also has an inlet 36 near the top with a valve 37.
  • gaseous reactants are introduced into the slurry of catalyst and liquid product via the gas distributor 18, maintaining the catalyst particles in suspension.
  • the correct temperature for reaction is maintained by the various sensors eg 24 and the heat transfer system 21,22,23.
  • Liquid product filters through the filter element 26 into the filtrate zone 28. This is encouraged by a pressure differential across the filter element caused by a hydrostatic head as a result of the difference in level between the slurry and the filtrate.
  • the level 34 of the filtrate is maintained constant by the vertical position of the horizontal section 33 of the outlet pipe 31.
  • the turbulent motion of the slurry helps to prevent the build-up of any filter cake and tends to avoid the filter element 26 becoming clogged with catalyst particles by causing fluctuations or oscillations in the pressure across the filter element 26 where the valve 39 is left open.
  • the filtration section 13 can be flushed, either by a suitable gas such as synthesis gas or a suitable liquid such as purified product, by opening the valve 37 and closing the valves 35 and 39. This forces the flushing fluid back through the filter element 26.
  • a suitable gas such as synthesis gas or a suitable liquid such as purified product
  • FIG. 2 An alternative constant level system for the filtrate is shown in Figure 2.
  • an annular weir 41 is provided within the housing 25.
  • the filtrate product collects between the filtrate element 26 and the weir 41 and overflows the weir.
  • the top of the weir determines the filtrate level 34.
  • An outlet 42 for the filtrate product is located in the housing 25 beyond the weir 41.
  • FIG. 3 A further embodiment of constant level device for the filtrate is shown in Figure 3.
  • the level 34 is set by a vertical outlet pipe 51 which extends upwards in the filtrate zone.
  • the filter element 103 is located within the reactor wall 14.
  • the filtration section housing is constituted by a portion 104 of the reactor wall 14.
  • the filtrate and any gas which may have passed through the filter element 103 will leave the filtration section 105 through a pipe 106 connected to the communication tube 38 and to an outlet 107 via a valve 108 controlled by a control unit 109.
  • Any sediment which may collect at the bottom of the filtrate section may be flushed out through a pipe 110 by opening a valve 111 when required.
  • Settling and flushing of sediments may be intentionally achieved (in this and other embodiments) by the appropriate dimensioning of the unit and by suitably designing the outlet.
  • the filter element 136 is located outside the reactor wall 14 but is otherwise housed with an external housing 25 as in Figure 1.
  • the reactor wall 14 is interrupted in the region of the filter element 136 by bars 131 which allow the slurry to contact the filter element 136.
  • the capacity can be increased by increasing the effective filter area.
  • One way of achieving this would be to replace the annular filter element 36 with a filter made up of a series of planar elements 61 as shown in Figure 6.
  • FIG. 7 shows such an arrangement in which there are three vertically spaced filtration sections 71,89,91. Each has a respective filter element 72, 82 and 92; an annular housing 73, 83 and 93; a filtrate zone 74, 84 and 94; a filtrate product outlet 75,85,95. Each outlet 75,85,85 includes an inverted U-shaped portion and in each case, the top of the S-shape defines a constant level for the filtrate in each respective zone 74,84,94.
  • Communication between the gas spaces above the filtrate zones 74,84,94 and the gas space 16 above the slurry zone 20 is provided by communication pipes 76,86,96 from each of the filtrate zones 74,84,94 which are connected to a common manifold 131.
  • the manifold 131 is connected to the gas space 16 via a valve 132.
  • the manifold 131 is also connected to those product outlets 75,85,95. Back flushing is carried out by shutting the vale 132 and the valves in lines 75, 85, 95, 76, 86, 96 and opening nitrogen inlet valves 77, 87 and 97.
  • FIG. 8 A similar alternative arrangement is shown in Figure 8.
  • the walls 88,78 terminate at different levels, thus determining the their respective constant filtrate levels 89,79.
  • the constant level 99 of the filtrate associated with the filter element 92 is determined by the position of the outlet 101.
  • the filtrate cascades over the walls 78 and 88 into the space defined by the housing 98 and the leaves via the common outlet 101.
  • FIG. 9 shows another embodiment in which a series of filtration sections 113 are used. Since the filtration sections 113 are identical in size and shape only one will be described.
  • the filtration section comprises an outer cylindrical wall 114 joined to the reaction vessel wall through flanges 115. Again, a filter element 116 is provided by a porous portion of the vessel wall. Thus, a filtrate zone 117 is defined.
  • Each filtration section 113 has a flushing fluid inlet 122 with a valve 123, connected to a common flushing fluid supply pipe 124.
  • a liquid outlet from the filtration zone 117 is provided by a tube 118 having a valve 119 controlled by a control unit 120.
  • a communication tube 121 is fitted to the upper part of the filtration zone 117 and the gas space 16 above the slurry (see Figure 1) via a common communication tube 125.
  • the open end of the common communication tube 125 extends into the space 16 above the slurry and is fitted with a valve 126, which is generally kept open during normal operation.
  • each of the communication tubes 121 may be fitted with valves (not shown) .
  • the communication tube 121 will allow any gas which would otherwise be trapped in the upper part of the filtration zone 117, to escape the gas space 16 above the slurry via the common communication tube 121 and the valve 126.
  • the control unit 120 connected to the valve 119 controls the flowrate of the liquid product from the filtration zone 117 in such a manner as to establish the mean pressure differential across the filter element 116.
  • the control unit will maintain the hydro ⁇ static pressure head on the filtrate side of the filter element 116 relative to the hydro-static pressure in the slurry phase, by maintaining the height of the liquid column in the communication tube 121 within a fixed range.
  • the control unit 120 may be provided with means (not shown) for detecting the liquid or pressure level in the communication tube 121.
  • the valve 119 will drain liquid product from the filtration zone 117 when an upper limit is detected by the sensory means of the control unit 120.
  • H f f H.P. - ⁇ P
  • ⁇ P is the small pressure differential required across the filter element 116.
  • ⁇ P would be given by ⁇ H ⁇ >.
  • ⁇ H is the additional slurry hydrostatic head responsible for the small pressure differential. While this relationship has been addressed in relation to the embodiment of Figure 9, it will be appreciated that it is, of course, generally applicable in all cases.
  • the vertical oscillatory motion of the filtrate in the pipe 121 enhances the tendency to dislodge catalyst particles adhering to the filter element 116 and helps to prevent agglomeration and the formation of a filter cake.
  • the filtration section 113 may be flushed by means of the flushing fluid inlet pipe 122 and valve 123.
  • the outlet valve 119 and common communication tube valve is 126 or alternatively, an individually fitted communication tube valve - not shown
  • the flushing fluid passes back through the filter 116.
  • the outlet valve 119 is opened, which allows a more rapid flow of the flushing fluid.
  • the entire reaction apparatus may be assembled from a small number of similar parts.
  • these components may be standard items which are generally available, such as standard tubing, flanges, valves etc.
  • assembly and disassembly would become very simple while the structure as a whole would be strong and rigid.
  • the main function of the cylindrical wall sections would be to contain the fluids within the reactor and to provide rigidity in the overall structure.
  • the required dimensions of the external parts (such as, the outer cylindrical walls 114, and in particular the flanges and their securing means) of the reactor shown in Figure 9 may become inconveniently large and impractical. Under such circumstances the entire reactor vessel assembly may be encapsulated within an external pressure hull (not shown) .
  • Figure 10 shows the measured separation capacity (kg/m 2 h) as a function of time on stream from the example described above.
  • the calculated pressure differential i.e. the driving force for the separation is also shown in Figure 10.
  • the mean value of this Figure is approximately 5 mbar. After 40 days on stream only a slight decrease in separation capacity was observed, and it was concluded that a separation capacity of at least 700 kg/m 2 h can be achieved for extended periods of time.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Combustion & Propulsion (AREA)
  • General Chemical & Material Sciences (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)

Abstract

Appareil (11) de mise en réaction d'une boue solide/liquide pour une synthèse de Fisher et Tropsch. La boue comporte un réacteur (12) délimitant une zone réactionnelle pour la phase boueuse située au-dessous d'un volume de gaz (16), une plaque (18) de fritte de gaz servant à introduire des réactifs gazeux dans la boue, et une partie de filtrage (13) agencée pour séparer le produit liquide de la boue. La partie de filtrage (13) comprend une enveloppe (25), un élément filtrant (26) et un conduit de sortie (32) pour le filtrat obtenu. Un tube (38) met en communication fluidique le volume de gaz (29) situé au-dessus du filtrat et le volume de gaz (16) situé au-dessus de la boue.
PCT/NO1994/000023 1993-01-28 1994-01-26 Appareil de traitement d'une boue solide/liquide et reacteur catalytique multi-phase WO1994016807A1 (fr)

Priority Applications (5)

Application Number Priority Date Filing Date Title
CA002154184A CA2154184C (fr) 1993-01-28 1994-01-26 Appareil de traitement solide/coulis liquide et reacteur catalytique multiphase
GB9515370A GB2289856B (en) 1993-01-28 1994-01-26 Solid/liquid slurry treatment apparatus and catalytic multi-phase reactor
AU60119/94A AU6011994A (en) 1993-01-28 1994-01-26 Solid/liquid slurry treatment apparatus and catalytic multi-phase reactor
DK199500849A DK172646B1 (da) 1993-01-28 1995-07-20 Apparat til behandling af en faststof/væskeopslæmning
NO952956A NO300799B1 (no) 1993-01-28 1995-07-26 Reaktor for kontinuerlig utförelse av en katalytisk flerfasereaksjon

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
GB9301723.4 1993-01-28
GB939301723A GB9301723D0 (en) 1993-01-28 1993-01-28 Solid/liquid treatment apparatus and catalytic multi-phase reactor

Publications (1)

Publication Number Publication Date
WO1994016807A1 true WO1994016807A1 (fr) 1994-08-04

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CN (1) CN1050533C (fr)
AU (1) AU6011994A (fr)
CA (1) CA2154184C (fr)
DK (1) DK172646B1 (fr)
DZ (1) DZ1750A1 (fr)
GB (2) GB9301723D0 (fr)
MY (1) MY134552A (fr)
WO (1) WO1994016807A1 (fr)
ZA (1) ZA94346B (fr)

Cited By (17)

* Cited by examiner, † Cited by third party
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WO1998050492A1 (fr) * 1997-05-06 1998-11-12 Exxon Research And Engineering Company Synthese d'hydrocarbures dans une suspension, avec filtration des produits achemines par un deversoir
WO1998051407A1 (fr) * 1997-05-16 1998-11-19 Exxon Research And Engineering Company Synthese d'hydrocarbures en suspension associee a une filtration externe des produits
EP0909581A1 (fr) * 1997-10-14 1999-04-21 AGIP PETROLI S.p.A. Reacteur pour reactions chimiques triphasiques
EP1177830A2 (fr) * 2000-07-31 2002-02-06 Nippon Shokubai Co., Ltd. Procédé de réaction en utilisant un catalyseur hétérogène et dispositif associé
US7067559B2 (en) 2001-07-03 2006-06-27 Shell Oil Company Process for the production of liquid hydrocarbons
WO2008074496A1 (fr) * 2006-12-21 2008-06-26 Eni S.P.A. Réacteur modulaire pour des réactions chimiques exothermiques et endothermiques
US7448601B2 (en) 2004-03-08 2008-11-11 Shell Oil Company Gas distributor for a reactor
EP2177260A1 (fr) 2008-10-06 2010-04-21 Global Bio-Chem Technology Group Company Limited Systèmes et procédés pour une réaction multiphase continue et séparation
WO2010139728A1 (fr) 2009-06-05 2010-12-09 Solvay Sa Procédé et dispositif d'extraction de liquide d'un mélange multiphase
US7919536B2 (en) 2006-05-31 2011-04-05 China Petroleum & Chemical Corporation Slurry bed loop reactor and use thereof
US20120003127A1 (en) * 2009-03-19 2012-01-05 Yasuhiro Onishi Catalyst separation system
EP2436438A1 (fr) * 2010-10-01 2012-04-04 Silicon Value LLC Réacteur à lit fluidisé
US8246915B2 (en) 2004-01-28 2012-08-21 Shell Oil Company Heat-exchanger for carrying out an exothermic reaction
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US20130171040A1 (en) * 2010-09-17 2013-07-04 Korea Research Institute Of Chemical Technology Reaction device for producing hydrocarbons from synthesis gas
US8580204B2 (en) 2011-04-20 2013-11-12 Siliconvalue Llc Fluidized bed reactor
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WO1998050492A1 (fr) * 1997-05-06 1998-11-12 Exxon Research And Engineering Company Synthese d'hydrocarbures dans une suspension, avec filtration des produits achemines par un deversoir
WO1998051407A1 (fr) * 1997-05-16 1998-11-19 Exxon Research And Engineering Company Synthese d'hydrocarbures en suspension associee a une filtration externe des produits
AU721272B2 (en) * 1997-05-16 2000-06-29 Exxon Research And Engineering Company Slurry hydrocarbon synthesis with external product filtration
EP0909581A1 (fr) * 1997-10-14 1999-04-21 AGIP PETROLI S.p.A. Reacteur pour reactions chimiques triphasiques
US6132690A (en) * 1997-10-14 2000-10-17 Agip Petroli S.P.A. Reactor for chemical reactions in triphasic systems having superimposed thermal exchange sections
EP1177830A2 (fr) * 2000-07-31 2002-02-06 Nippon Shokubai Co., Ltd. Procédé de réaction en utilisant un catalyseur hétérogène et dispositif associé
EP1177830A3 (fr) * 2000-07-31 2003-04-02 Nippon Shokubai Co., Ltd. Procédé de réaction en utilisant un catalyseur hétérogène et dispositif associé
US6610879B2 (en) 2000-07-31 2003-08-26 Nippon Shokubai Co., Ltd. Reaction method by using heterogeneous catalyst and reaction apparatus therefor
US7067559B2 (en) 2001-07-03 2006-06-27 Shell Oil Company Process for the production of liquid hydrocarbons
US8377707B2 (en) 2003-06-20 2013-02-19 Roche Diagnostics Operations, Inc. System and method for determining an abused sensor during analyte measurement
US8246915B2 (en) 2004-01-28 2012-08-21 Shell Oil Company Heat-exchanger for carrying out an exothermic reaction
US7448601B2 (en) 2004-03-08 2008-11-11 Shell Oil Company Gas distributor for a reactor
US7919536B2 (en) 2006-05-31 2011-04-05 China Petroleum & Chemical Corporation Slurry bed loop reactor and use thereof
US8263007B2 (en) 2006-05-31 2012-09-11 China Petroleum Chemical Corporation Slurry bed loop reactor and use thereof
WO2008074496A1 (fr) * 2006-12-21 2008-06-26 Eni S.P.A. Réacteur modulaire pour des réactions chimiques exothermiques et endothermiques
US8092747B2 (en) 2006-12-21 2012-01-10 Eni S.P.A. Modular reactor for exothermic/endothermic chemical reactions
EP2177260A1 (fr) 2008-10-06 2010-04-21 Global Bio-Chem Technology Group Company Limited Systèmes et procédés pour une réaction multiphase continue et séparation
US20120003127A1 (en) * 2009-03-19 2012-01-05 Yasuhiro Onishi Catalyst separation system
US8524160B2 (en) * 2009-03-19 2013-09-03 Japan Oil, Gas And Metals National Corporation Catalyst separation system
WO2010139728A1 (fr) 2009-06-05 2010-12-09 Solvay Sa Procédé et dispositif d'extraction de liquide d'un mélange multiphase
US8758612B2 (en) 2009-06-05 2014-06-24 Solvay Sa Process and device for separating liquid from a multiphase mixture
US20130171040A1 (en) * 2010-09-17 2013-07-04 Korea Research Institute Of Chemical Technology Reaction device for producing hydrocarbons from synthesis gas
US9266080B2 (en) * 2010-09-17 2016-02-23 Korea Research Institute Of Chemical Technology Reaction device for producing hydrocarbons from synthesis gas
EP2436438A1 (fr) * 2010-10-01 2012-04-04 Silicon Value LLC Réacteur à lit fluidisé
US8580203B2 (en) 2010-10-01 2013-11-12 Siliconvalue Llc Fluidized bed reactor
US9937476B2 (en) * 2010-12-13 2018-04-10 Sasol Technology (Proprietary) Limited Slurry phase apparatus
US10322393B2 (en) 2010-12-13 2019-06-18 Sasol Technology (Proprietary) Limited Slurry phase apparatus
US8580204B2 (en) 2011-04-20 2013-11-12 Siliconvalue Llc Fluidized bed reactor

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GB2289856B (en) 1997-06-04
CN1092337A (zh) 1994-09-21
DK172646B1 (da) 1999-04-06
GB9301723D0 (en) 1993-03-17
GB2289856A (en) 1995-12-06
MY134552A (en) 2007-12-31
DZ1750A1 (fr) 2002-02-17
AU6011994A (en) 1994-08-15
CA2154184A1 (fr) 1994-08-04
CN1050533C (zh) 2000-03-22
DK84995A (da) 1995-09-27
CA2154184C (fr) 2004-03-23
GB9515370D0 (en) 1995-10-04
ZA94346B (en) 1995-07-18

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