• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    The invention relates to a method for producing an oil rich fraction (OF) from primary feedstock (FS) that comprises water, first salt, second salt, and biomass. The feedstock (FS) is provided to a first reaction zone (Z1) of a conversion reactor (100), where it is allowed to react at a temperature of at least 350 °C in a pressure of at least 160 bar to form converted primary feedstock. The method comprises separating from the converted primary feedstock a first salt rich fraction (SF1), a second salt rich fraction (SF2), and an oil rich fraction (OF). The method comprises withdrawing the oil rich fraction (OF) from the first reaction zone (Z1) and withdrawing the first salt rich fraction (SF1) and the second salt rich fraction (SF2) from the conversion reactor (100). In the method the first salt rich fraction (SF1) comprises at least some of the first salt dissolved in the water, the second salt rich fraction (SF2) comprises at least some of the second salt in solid form, and at least one of the first salt and the second salt is a salt capable of catalysing the reaction of the biomass of the primary feedstock (FS) with the water of the primary feedstock (FS) to produce the oil rich fraction (OF). A device for the same.
    公开号:FI20195955A1
    申请号:FI20195955
    申请日:2019-11-08
    公开日:2021-05-09
    发明作者:Tero Joronen
    申请人:Valmet Technologies Oy；
    IPC主号:
    专利说明:

    [1] [1] Thomas Voisin, Arnaud Erriguible, David Ballenghien, David Mateos, André Kunegel, et al.. Solubility of inorganic salts in sub- and supercritical hydrothermal environment. Application to SCWO processes. Journal of Supercritical — Fluids, Elsevier, 2017, 120, Part 1, pp.18-31. = 10.1016/j.supflu.2016.09.020. hal-01417006
    N 3 30 i 3ON
    权利要求:
    Claims (18)
    [1] 1. A method for producing an oil rich fraction (OF) from biomass, the method comprising - providing primary feedstock (FS) that comprises water, first salt, second salt, and biomass to a first reaction zone (Z1) of a conversion reactor (100), - allowing the primary feedstock (FS) to react in the first reaction zone (Z1) at a temperature of at least 350 °C in a pressure of at least 160 bar to form converted primary feedstock, - separating at the temperature of at least 350 °C and in the pressure of at least 160 bar from the converted primary feedstock a first salt rich fraction (SF1), a second salt rich fraction (SF2), and an oil rich fraction (OF), - withdrawing the oil rich fraction (OF) from the first reaction zone (Z1), and - withdrawing the first salt rich fraction (SF1) and the second salt rich fraction (SF2) from the conversion reactor (100), wherein - the first salt rich fraction (SF1) comprises at least some of the first salt dissolved in the water, - the second salt rich fraction (SF2) comprises at least some of the second salt in solid form, and - at least one of the first salt and the second salt is a salt capable of catalysing the reaction of the biomass of the primary feedstock (FS) with the water of the primary feedstock (FS) to produce the oil rich fraction (OF).
    [2] 2. The method of claim 1, wherein at least one of the first salt and the second = salt is a salt of ametal having a standard electrode potential at the temperature N 298 K of at most -0.5 V; preferably at most -1.5 V; - preferably 3 30 - the first salt is a salt of a metal having a standard electrode potential at the I temperature 298 K of at most -1.5 V; so more preferably 3 - the first salt is a salt of potassium (K) or sodium (Na). > N 35 3. The method of claim 1 or 2, wherein a total content of the first and second salts of the primary feedstock (FS) is at least 1 wt%, preferably from 5 wt% to 40 wt%;
    [3] preferably - a total content of the first and second salt(s) of the dry matter of the primary feedstock (FS) is at least 1 wt%, preferably from 5 wt% to 40 wt%; more preferably, - the primary feedstock (FS) comprises at least 1 wt% ions of sodium and/or potassium; even more preferably, - the dry matter of the primary feedstock (FS) comprises at least 1 wt% ions of sodium and/or potassium.
    [4] 4. The method of any of the claims 1 to 3, comprising - feeding at least some of the first salt rich fraction (SF1) and/or at least some of the second salt rich fraction (SF2) into the first reaction zone (Z1) of the conversion reactor (100); preferably - at least some of the first salt rich fraction (SF1) is fed into the first reaction zone (Z1) of the conversion reactor (100).
    [5] 5. The method of any of the claims 1 to 4, wherein - the primary feedstock (FS) comprises black liquor and the method comprises - feeding at least some of the first salt rich fraction (SF1) and/or at least some of the second salt rich fraction (SF2) into chemical recovery cycle configured to recover cooking chemicals; preferably - at least some of the second salt rich fraction (SF2) is fed into the chemical recover cycle. 2 N
    [6] 6. The method of any of the claims 1 to 5, comprising - - cooling at least one of the oil rich fraction (OF) and a reaction product (RP) 3 30 of the oil rich fraction (OF) — preferably to a temperature from 5 °C to 95 °C I — to produce liquid bio oil (OIL); so preferably the method further comprises S - separating at least one of a non-condensable gas (NCG) and a water rich 3 fraction (WF) from the condensate of the oil rich fraction (OF) or the reaction product (RP) thereof to produce the liquid bio oil (OIL).
    [7] 7. The method of the claim 6, comprising - recovering heat from the oil rich fraction (OF) or a reaction product (RP) thereof to produce the liquid bio-oil (OIL) and - heating at least a part of the primary feedstock (FS) with the recovered heat.
    [8] 8. The method of any of the claims 1 to 7, wherein - an oxygen content of the oil rich fraction (OF) is at most 20 wt%, preferably at most 15 wt% and/or - an oxygen content of the bio-oil (OIL) of claim 6 or 7 is at most 20 %, preferably at most 15 %.
    [9] 9. The method of claim any of the claims 1 to 8, comprising - allowing the primary feedstock (FS) to react in the first reaction zone (Z1) at a temperature from 350 °C to 450 °C in a pressure of from 220 bar to 350 bar for at least 5 minutes.
    [10] 10. The method of any of the claims 1 to 9, comprising - crystallizing at least a part of the second salt in a crystallizer (310) to from crystallized second salt.
    [11] 11. The method of any of the claims 1 to 10, comprising - crystallizing at least a part of the second salt onto solid particles (410); preferably the method comprises - crystallizing at least a part of the second salt onto solid particles (410) having a density that deviates from a density of the materials in the first reaction zone (Z1) by at most 25 %. = more preferably the method comprises N - crystallizing at least a part of the second salt onto hollow metal particles. 3 30 12. The method of any of the claims 1 to 11, comprising z - transferring the oil rich fraction (OF) to a second reaction zone (Z2) and so - allowing the oil rich fraction to (OF) react in the presence of a solid catalyst S (CAT) in the second reaction zone (Z2) to produce the reaction product (RP); 3 optionally the method comprises - feeding also hydrogen (H>) to the second reaction zone (Z2) and - allowing the oil rich fraction (OF) and the hydrogen (Hy) to react in the second reaction zone (Z2);
    [12] preferably, - the solid catalyst (CAT) has at least a deoxygenating functionality.
    [13] 13. A system for producing an oil rich fraction (OF) from biomass, the system comprising - a conversion reactor (100) configured to allow a primary feedstock (FS) to react in a first reaction zone (Z1) at a temperature of at least 350 °C in a pressure of at least 160 bar to form converted primary feedstock, the conversion reactor (100) comprising e a first inlet (101) for letting in the primary feedstock (FS) into the first reaction zone (Z1), e a first outlet (103) for letting out a first salt rich fraction (SF1) from the conversion reactor (100), the first salt rich fraction (SF1) comprising first salt dissolved in water, e a second outlet (104) for letting out a second salt rich fraction (SF2) from the conversion reactor (100), the second salt rich fraction (SF2) comprising second salt in solid form, and e a third outlet (105) for letting out at least one of the oil rich fraction (OF) and a reaction product (RP) of the oil rich fraction (OF) from the conversion reactor (100), wherein e the conversion reactor (100) is configured to separate a first salt rich fraction (SF1), a second alt rich fraction (SF2), and the oil rich fraction (OF) from the converted primary feedstock at the temperature of at least 350 *C and in the pressure of at least 160 bar, the system comprising -apump (120) configured to pump the primary feedstock (FS) through the first inlet (101) to the a first reaction zone (21) having the pressure of at least = 160 bar, and N - a heater (130) configured to heat at least one of the primary feedstock (FS), - the conversion reactor (100), a recycled part of the first salt rich fraction (SF1) 3 30 and a recycled part of the second salt rich fraction (SF2) such that a x temperature in the first reaction zone (Z1) is at least 350 °C. O
    [14] 14. The system of claim 13, comprising
    LO O - a cooler (110) configured to cool at least one of the oil rich fraction (OF) and | 35 a reaction product (RP) of the oil rich fraction (OF) to produce liquid bio oil (OIL), and
    - a pipeline (112) for conveying at least one of the oil rich fraction (OF) and the reaction product (RP) to the cooler (110).
    [15] 15. The system of claim 13 or 14, wherein - the conversion reactor (100) comprises a crystallizer (310) configured to crystallize a salt of the feedstock (FS) and - the crystallizer (310) comprises the second outlet (104).
    [16] 16. The system of any of the claims 13 to 15, comprising - a vessel (420) configured to receive the second salt rich fraction (SF2), wherein in the vessel (420), solid particles (410) covered by solidified salt are configured to be washed and - a line (422) configured to convey washed solid particles from the vessel (420) to the conversion reactor (100).
    [17] 17. The system of any of the claims 13 to 16, comprising - solid catalyst material (CAT) in a second process zone (Z2) of the conversion reactor (100) or of a catalytic reactor (200), the solid catalyst (CAT) being configured to convert the oil rich fraction (OF) to a reaction product (RP); preferably, the system comprises - a second inlet (102) for letting in hydrogen into the second process zone (Z2).
    [18] 18. The system of any of the claims 13 to 17, comprising - a chemical recovery boiler (500) configured to burn black liquor, - a first pipeline configured to convey black liquor to the first inlet (101), and - a pipeline arrangement configured to convey at least a part of the first salt = rich fraction (SF1) and/or at least a part of the second salt rich fraction (SF2) N to the chemical recovery boiler (500); - preferably, 3 30 - the pipeline arrangement is configured to convey at least a part of the second z salt rich fraction (SF2) to the chemical recovery boiler (500); so preferably the system comprises S - a second pipeline configured to convey black liquor to the chemical recovery 3 boiler (500), wherein N 35 - the second pipeline comprises a branch, such that a part of the black liguor is configured to be conveyed to the chemical recovery boiler (500) and a part of the black liquor configured to be conveyed to the first inlet (101) through the branch and the first pipeline.
    oO
    O
    N o
    O
    I =
    LO
    LO o
    LO o
    O
    N
    类似技术:
    公开号 | 公开日 | 专利标题
    US4470876A|1984-09-11|Kraft overload recovery process
    US6007636A|1999-12-28|Method to recycle an aqueous acidic liquor used for depolymerization of cellulose
    RU2696962C2|2019-08-07|Incorporated system of kraft-pulp plant and thermochemical transformation
    US20140127786A1|2014-05-08|Process and apparatus for producing liquid hydrocarbon
    EP3114229A1|2017-01-11|Production of products with favourable ghg emission reductions from cellulosic feedstocks
    US3762989A|1973-10-02|Pyrolysis of spent pulping liquors
    US5286845A|1994-02-15|Acidification of tall oil soap using carbon dioxide
    US3607619A|1971-09-21|Coking of black liquor in the absence of added free oxygen
    US20030221804A1|2003-12-04|Lignins derived from black liquor
    DE102013217418A1|2014-11-13|Hydrothermal treatment of sewage sludge and black liquor
    FI129246B|2021-10-15|A method and a system for producing an oil rich fraction from biomass
    US3558426A|1971-01-26|Treatment of waste liquors from pulp and paper mills
    US4329199A|1982-05-11|Process for digesting and bleaching cellulosic material with reduced emissions
    AU2013203860B2|2015-01-29|Method of recovering pulping chemicals and reducing the concentration of potassium and chloride therein
    FI70057C|1986-09-12|FOERFARANDE FOER BEHANDLING AV SVARTLUT
    JP2006257577A|2006-09-28|Method for gasifying kraft pulp black liquor and method for producing hydrogen
    AU2016271293B2|2018-10-04|Method of recovering pulping chemicals from dissolved ash having a high carbonate content
    SE540646C2|2018-10-09|Method and system for treating spent pulping liquor
    Jahan et al.2016|Dissolving pulp from white press cuttings
    US10533138B2|2020-01-14|Recovery system for high pressure processing system
    Wilke et al.2021|Integrated Forest Biorefinery: A Proposed Pulp Mill of 2040
    US1580269A|1926-04-13|Process for regenerating black liquor
    Kilpi2019|Reduction of sulfate emissions in bleached softwood kraft pulp mill
    CA2133663C|2006-07-18|Improved acidification of tall oil soap using carbon dioxide
    WO2021121662A1|2021-06-24|Product separation & purification method and system
    同族专利:
    公开号 | 公开日
    WO2021089923A1|2021-05-14|
    FI129246B|2021-10-15|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    CN204939232U|2015-09-10|2016-01-06|新奥科技发展有限公司|Supercritical reaction device and supercritical reaction system|
    法律状态:
    2021-10-15| FG| Patent granted|Ref document number: 129246 Country of ref document: FI Kind code of ref document: B |
    优先权:
    申请号 | 申请日 | 专利标题
    FI20195955A|FI129246B|2019-11-08|2019-11-08|A method and a system for producing an oil rich fraction from biomass|FI20195955A| FI129246B|2019-11-08|2019-11-08|A method and a system for producing an oil rich fraction from biomass|
    PCT/FI2020/050735| WO2021089923A1|2019-11-08|2020-11-06|A method and a system for producing an oil rich fraction from biomass|
    [返回顶部]