An apparatus and method of removing a selected component from a stream of fluid containing a plurality of components is provided. The stream is induced to flow at supersonic velocity through a conduit so as to decrease the temperature of the fluid to below a selected temperature at which one of cond
An apparatus and method of removing a selected component from a stream of fluid containing a plurality of components is provided. The stream is induced to flow at supersonic velocity through a conduit so as to decrease the temperature of the fluid to below a selected temperature at which one of condensation and solidification of the selected component occurs, thereby forming particles of the selected component. The conduit is provided with a structure for imparting a swirling motion to the stream of fluid thereby inducing the particles to flow to a radially outer section of a collecting zone in the stream. A shock wave is created in the stream so as to decrease the axial velocity of the fluid to subsonic velocity, and to increase the swirling motion of the particles which are extracted into an outlet stream from the radially outer section of the collecting zone downstream of the shock wave.
대표청구항▼
An apparatus and method of removing a selected component from a stream of fluid containing a plurality of components is provided. The stream is induced to flow at supersonic velocity through a conduit so as to decrease the temperature of the fluid to below a selected temperature at which one of cond
An apparatus and method of removing a selected component from a stream of fluid containing a plurality of components is provided. The stream is induced to flow at supersonic velocity through a conduit so as to decrease the temperature of the fluid to below a selected temperature at which one of condensation and solidification of the selected component occurs, thereby forming particles of the selected component. The conduit is provided with a structure for imparting a swirling motion to the stream of fluid thereby inducing the particles to flow to a radially outer section of a collecting zone in the stream. A shock wave is created in the stream so as to decrease the axial velocity of the fluid to subsonic velocity, and to increase the swirling motion of the particles which are extracted into an outlet stream from the radially outer section of the collecting zone downstream of the shock wave. tion with a solvent selective for cobalt or nickel in order to obtain a respective product with a Co:Ni or Ni:Co ratio≥400:1; (f) separating the nickel and cobalt using an ion-exchange resin with HSO2functional groups through various countercurrent stages with an efficiency of 99.5%; and (g) separating 40-95 wt. % of cobalt with a Ni:Co ratio from 2:1 to 4:1 by one selected from ammonium hydrosulphide, H2S and Na2S. 8. The process of claim 2, further comprising at least one of additional steps selected from the additional steps comprising of: (a) leaching the pulp in turbo aerators and liquid/solid separation equipment; (b) flash liquid/solid separating the pulp in equipment means including hydroclones and a thickener, thereby reducing the liquor-solid contact time, to a pulp density of 40-60 wt. % solids; (c) reextracting and washing in a tubular reactor of 0.5-10 wt. % nickel and 2-25 wt. % cobalt contained in the solid for 0.5-20 minutes; (d) washing in a tubular reactor of the ammonia contained in the pulp for 0.5-20 minutes; (e) separating the nickel and cobalt from the pregnant liquor by extraction with a solvent selective for cobalt or nickel in order to obtain a respective product with a Co:Ni or Ni:Co ratio≥400:1; (f) separating the nickel and cobalt using an ion-exchange resin with HSO2functional groups through various countercurrent stages with an efficiency of 99.5%; and (g) separating 40-95 wt. % of cobalt with a Ni:Co ratio from 2:1 to 4:1 by one selected from ammonium hydrosulphide, H2S, and Na2S. 9. The process of claim 3, further comprising at least one of additional steps selected from the additional steps comprising of: (a) leaching the pulp in turbo aerators and liquid/solid separation equipment; (b) flash liquid/solid separating the pulp in equipment means including hydroclones and a thickener, thereby reducing the liquor-solid contact time, to a pulp density of 40-60 wt. % solids; (c) reextracting and washing in a tubular reactor of 0.5-10 wt. % nickel and 2-25 wt. % cobalt contained in the solid for 0.5-20 minutes; (d) washing in a tubular reactor of the ammonia contained in the pulp for 0.5-20 minutes; (e) separating the nickel and cobalt from the pregnant liquor by extraction with a solvent selective for cobalt or nickel in order to obtain a respective product with a Co:Ni or Ni:Co ratio≥400:1; (f) separating the nickel and cobalt using an ion-exchange resin with HSO2functional groups through various countercurrent stages with an efficiency of 99.5%; and (g) separating 40-95 wt % of cobalt with a Ni:Co ratio from 2:1 to 4:1 by one selected from ammonium hydrosulphide, H2S, and Na2S. 10. The process of claim 4, further comprising at least one of additional steps selected from the additional steps comprising of: (a) leaching the pulp in turbo aerators and liquid/solid separation equipment; (b) flash liquid/solid separating the pulp in equipment means including hydroclones and a thickener, thereby reducing the liquor-solid contact time, to a pulp density of 40-60 wt. % solids; (c) reextracting and washing in a tubular reactor of 0.5-10 wt. % nickel and 2-25 wt. % cobalt contained in the solid for 0.5-20 minutes; (d) washing in a tubular reactor of the ammonia contained in the pulp for 0.5-20 minutes; (e) separating the nickel and cobalt from the pregnant liquor by extraction with a solvent selective for cobalt or nickel in order to obtain a respective product with a Co:Ni or Ni:Co ratio≥400:1; (f) separating the nickel and cobalt using an ion-exchange resin with HSO2functional groups through various countercurrent stages with an efficiency of 99.5%; and (g) separating 40-95 wt.-% of cobalt with a Ni:Co ratio from 2:1 to 4:1 by one selected from ammonium hydrosulphide, H2S, and Na2S. 11. The process of claim 5, further comprising at lea st one of additional steps selected from the additional steps comprising of: (a) leaching the pulp in turbo aerators and liquid/solid separation equipment; (b) flash liquid/solid separating the pulp in equipment means including hydroclones and a thickener, thereby reducing the liquor-solid contact time, to a pulp density of 40-60 wt. % solids; (c) reextracting and washing in a tubular reactor of 0.5-10 wt. % nickel and 2-25 wt. % cobalt contained in the solid for 0.5-20 minutes; (d) washing in a tubular reactor of the ammonia contained in the pulp for 0.5-20 minutes; (e) separating the nickel and cobalt from the pregnant liquor by extraction with a solvent selective for cobalt or nickel in order to obtain a respective product with a Co:Ni or Ni:Co ratio≥400:1; (f) separating the nickel and cobalt using an ion-exchange resin with HSO2functional groups through various countercurrent stages with an efficiency of 99.5%; and (g) separating 40-95 wt. % of cobalt with a Ni:Co ratio from 2:1 to 4:1 by one selected from ammonium hydrosulphide, H2S, and Na2S. 12. The process of claim 6, further comprising at least one of additional steps selected from the additional steps comprising of: (a) leaching the pulp in turbo aerators and liquid/solid separation equipment; (b) flash liquid/solid separating the pulp in equipment means including hydroclones and a thickener, thereby reducing the liquor-solid contact time, to a pulp density of 40-60 wt. % solids; (c) reextracting and washing in a tubular reactor of 0.5-10 wt. % nickel and 2-25 wt. % cobalt contained in the solid for 0.5-20 minutes; (d) washing in a tubular reactor of the ammonia contained in the pulp for 0.5-20 minutes; (e) separating the nickel and cobalt from the pregnant liquor by extraction with a solvent selective for cobalt or nickel in order to obtain a respective product with a Co:Ni or Ni:Co ratio≥400:1; (f) separating the nickel and cobalt using an ion-exchange resin with HSO2functional groups through various countercurrent stages with an efficiency of 99.5%; and (g) separating 40-95 wt. % of cobalt with a Ni:Co ratio from 2:1 to 4:1 by one selected from ammonium hydrosulphide, H2S, and Na2S. 13. The process according to claim 1, where the pressure is 1.5 to 10.0 bar at the inlet of the tubular reactor. 14. The process according to claim 2, where the pressure is 1.5 to 10.0 bar at the inlet of the tubular reactor. 15. The process according to claim 3, where the pressure is 1.5 to 10.0 bar at the inlet of the tubular reactor. 16. The process according to claim 4, where the pressure is 1.5 to 10.0 bar at the inlet of the tubular reactor. 17. The process according to claim 5, where the pressure is 1.5 to 10.0 bar at the inlet of the tubular reactor. 18. The process according to claim 6, where the pressure is 1.5 to 10.0 bar at the inlet of the tubular reactor. 19. The process according to claim 7, where the pressure is 1.5 to 10.0 bar at the inlet of the tubular reactor. 20. The process of claim 1, further comprising cooling the leached pulp in the tubular reactor so that the temperature increases no more than 1 to 6° C.
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이 특허에 인용된 특허 (4)
Linhardt Hans D. (Newport Beach CA) Beveridge John H. (San Clemente CA), Curved duct separator for removing particulate matter from a carrier gas.
Lardinois Jean-Paul (Rue des Champs No. 15 5030 Gemblaux BEX), Process for extraction of a substance from a gaseous carrier gas, as solid or liquid particles and system to operate the.
Betting, Marco; Brouwer, Jacob Michiel; van Eck, Pascal; Tjeenk Willink, Cornelis Antonie, Method and system for cooling a natural gas stream and separating the cooled stream into various fractions.
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