• 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:
    Continuously operating separating apparatus for the separation of mixtures of light and heavy liquid components, which apparatus comprises a mixing portion, which is located in the middle portion of said apparatus and which comprises a mixing vessel and a cylinder placed in the middle of said mixing vessel, and a separating portion, which is located in the upper portion of said apparatus and which comprises two or more cones placed one inside the other, and a circulating pump, which is connected by means of two or more conduits tangentially to said mixing vessel, and a bottom portion, and a feed conduit, which is connected tangentially to the upper portion of said mixing vessel, and discharge members located in the upper portion of said apparatus, said discharge members comprising an overflow member and discharge outlets, through which the light liquid fraction is discharged, and a substantially vertical discharge member placed in the middle of said apparatus, through which member the heavy liquid fraction is discharged.
    公开号:SU1574162A3
    申请号:SU843686254
    申请日:1984-01-04
    公开日:1990-06-23
    发明作者:Линдквист Ханс；Гренберг Видар
    申请人:Линотек Ой (Фирма)；
    IPC主号:
    专利说明:

    The invention relates to a continuously operating device for the separation of mixtures of light to heavy liquid components and a continuous process.
    separating gall oil from acidified gall oil soap mixture
    The purpose of the invention is to increase the reliability and efficiency of work.
    Figure 1 is a diagram of the proposed device: figure 2 is the same, a general view with a partial cut; figure 3 is the same section; Fig. 4 is a schematic of a device with fluid circulation means.
    The device contains a vertically mounted vessel 1 with a receiving bottom part 2, a mixing part 3 placed in the middle part of the vessel, a separating part 4, a fluid supply means 5 tangentially attached to the vessel, outlet elements for discharging the light fraction, containing a discharge element 6, collective pipes 7, exhaust pipes 8 and a ventilation pipe 9. The bottom part 2 has a conical shape, and a pipe 10 is provided in the lei for discharging sludge.
    An exhaust element for unloading a heavy component is located inside a cylinder 11 vertically mounted in the center of the mixing part 3 and comprises a discharge pipe 12E, a sliding pipe 13 located in its upper part, and an adjusting element 14 for the sliding rough. In the casing of the mixing part 3 there are one or several viewing stacks 15, and in the lid of the separation section there are several and preferably four control holes 16. In the mixing part 3, the mixture is intensively circulated using a circulation pump 17, as indicated by arrow 18. From there light components moving up (arrow 19), and heavy components moving down (arrow 20). The circulating pump I7 is connected to the mixing part 3 by means of the pipelines 21 and 22 that are installed at the price. By adjusting the slide pipe 13 by means of the adjusting element 14, the interface between the phases can be maintained at the required level, which is 0-50 cm above the upper edge site mix. In the separation area, droplets of the heavy phase are effectively separated from the light phase and flow down the building itself 23, located one inside the other along the vertical axis at some distance from each other,
    ,,
    ten
    jc - .n
    41624
    0-200 mm and constituting a number of channels 24 for the light fraction. The cone angle at the apex is less than 90 °. Gas and water vapor are discharged through a vent pipe 9 located at the top of the device. Unloading of heavy materials like gypsum, accumulating at the bottom of the device, takes place through pipe 10 going through the bottom.
    The removal of the heavy phase, so that the interface between the light and heavy fractions remains at a level of 0-0.5 m above the top edge of the mixing part 3, is carried out using an adjustable retractable pipe 13 or by means of control valves, as well as two or more switches 28 and 29. The diameter of the cylinder 11 is 1/2

    / 5 diameter mixing part 3 of the tank.
    A vertical exhaust element (exhaust pipe 12} is located in the middle of the vessel 1, and its inlet end 30 is located concentrically inside the vertical cylinder 11.
    Example 1
    35
    40
    55
    tall soap, obtained by mixing 1300 kg / h of tall oil foam, separated from black liquor and 560 kg / h of 30% sulfuric acid. The mixture contains,%: tall oil (density 960 kg / m3) 45; the mother liquor (density 1106 kg / m3, pH 3.2) 45; and lignin 8, as well as gypsum 2. The speed of 1860 kg / h at 90 ° C. The mixture entered tangentially through 45 the fluid supply means 5 into the mixing part 3 of the device, where the mixture was circulated by means of a circulation pump 17 tangentially connected via pipes 21 and 22,. rotational movement was reported in space bounded by vessel 1 and cylinder 11 located in the center of the vessel. The circulation rate is 23 m / h. Top unloaded tall oil through the elements of 6-8. The mother liquor and the lignin dispersed therein flowed into the exhaust pipe 12 and were discharged from the bottom of the device.
    50
    The sliding tube 13, located at the top of the exhaust pipe 12, was adjusted so that the interface between tall oil and mother liquor was approximately at the level of the upper edge of the mixing part 3.
    Analysis of the separated tall oil, vol.%:
     Gall oil 97
    Lignin3
    Gypsum stock solution
    Analysis of the separated stock solution, vol.%:
    Tall oil 2
    S
    Lignin
    Uterine Solution 96
    Gypsum1
    Example2. The separating device of Example 1 was supplied with a mixture of tall soap obtained by mixing 820 kg / h of tall oil foam separated from black liquor, and 6) 0 kg / h of spent acid produced in the production of chlorine dioxide having a composition, g / l: sodium sulfate 360; sulfuric acid (100%) 456 sodium chlorate about 3. The mixture contained,%: tall oil (density 960 kg / m3) 55; the mother liquor (density 1106 kg / m) 40; lignin (density 1600 kg / m) 45 and also gypsum less than 1. The mixture was supplied at a rate of 1430 kg / h at 90QC. She passed tangentially into the mixing part 3 of the device, where the circulation intensity was 19.5 me / h. On top of the device, unloading of tall oil through drain element 6 occurred. The mother liquor and lignin dispersed therein flowed into exhaust pipe 12 and were discharged from below the device. Sliding pipe 13 located in the upper part of exhaust pipe 12 was adjusted so that the boundary surface between tall oil and the mother liquor was 0.1 m above the upper edge of the mixing part.
    Analysis of the separated tall oil, vol.%:
    Tall oil 98
    Lignin2
    Mother solution
    Gypsum
    Analysis of the separated stock solution, vol.%:
    6
    Tall oil 2
    Lignin4
    The mother liquor 94 GypsumPrimerZ. The separation device of example 1 was supplied with a mixture of tall oil, obtained by mixing 1715 kg / h of tall oil foam 0 separated from black liquor, and 415 kg / h of spent acid obtained in the production of chlorine dioxide, of the following composition, g / l: sodium sulfate 360, sulfuric acid 5 (100%) 456 and sodium chlorate about 3. The mixture contained,%: tall oil C density, 960 kg / m3) 25; the mother liquor (density kg / m, pH 2.2) 70; lignin 0 (density 1060 kg / m) 4, as well as gypsum 1. The mixture was fed at a speed of 2130 kg / h at 94 ° C. The mixture tangentially entered the mixing part.
    five
    0
    five
    0
    five
    3 devices, where the circulation rate is 24 m / h. Tall oil flowed from the top of the device through the discharge element 6. The mother liquor and the lignin dispersed therein flowed into the exhaust pipe 12 and were discharged from the bottom of the device. The sliding tube 13, located on top of the exhaust pipe 12, was adjusted so that the interface between tall oil and the mother liquor was 0.3 m above the top edge of the mixing part 3.
    Analysis of separated tall oil,. vol.%: Tall oil 95
    Lignin3
    The mother solution 1
    Gypsum1
    Analysis of the separated mother liquor, vol.%: Tall oil 2
    Lignin2
    Royal solution 94
    Gypsum2
    Example p4. A separating device with a volume of approximately 1.7 m3 (mixing part of approximately 0.6 m, a separation section of approximately 1 m3 and a bottom cone of approximately 0.1 m) was fed a mixture containing,%: tall oil (density 950 kg / m3) 32; mother liquor (density 1100 kg / m
    , 0) 62; lignin (density 1060 kg / m 6. The speed of 600 kg / h at 80 ° С.

    The mixture entered tangentially through the fluid supply means 5 into the mixing part 3 of the device, where, using a recirculation pump 17 tangentially connected to the mixing tank, the mixture reported rotational movement in the space bounded by the tank casing and the cylinder 11 located in the center of the tank. The circulation rate is 16 m3 / h. Tall oil was discharged from the top through elements 6-8. The mat solution and the lignin dispersed in it flowed into the tube 12 and were unloaded from the bottom of the device. The sliding tube 13, located in the upper part of the exhaust tube 12, was adjusted so that the interface between tall oil and mother liquor was approximately at the level of the upper one. edge mixing part.
    Analysis of separated Ualsva oil, vol. %: Tall oil 98 Lignin 1 Uterine solution 2 Gypsum - Analysis of the separated mother liquor of the thief;
    Tall oil 2 Lignin2
    96 Gypsum stock solution
    EXAMPLE 5 The separation device of Example 4 was used in the same operations. The composition of the feed mixture, vol.%: Tall oil (density 950 kg / m) 30; mother liquor (density 1105 kg / m, pH 3.0) 63; lignin (with a density of 1060 kg / m3) 7. A feed rate of 1000 kg / h at 87 C. A circulation rate of 17 m / h.
    Analysis of the separated tall oil, vol.%:
    Tall oil 99 Lignin1
    The mother liquor - Gypsum
    Analysis of the separated stock solution, vol.%:
    Tall oil 2 Lignin3
    Uterine Solution 95 Gypsum
    PRI me R 6. Used separation device according to example 4

    0
    0 5
    five
    0
    five
    on the same operations. The composition of the feed mixture, vol.%: Tall oil (density 950 kg / m) 32; the mother liquor (density 1110 kg / m, rI 3,0) 60; lignin (density 1060 kg / m) 8. Feed rate 1530 kg / h at 87 C. Circulation speed 20 m / h.
    Analysis of the separated tall oil, vol. %:
    Tall oil 98
    Lignin1
    The mother solution 1
    Gypsum
    Analysis of the separated mother liquor, vol.%: “Tall oil 2
    Lignin3
    Uterine Solution 95
    Gypsum
    Example. The separation device of Example 4 was used in the same operations. The composition of the feed mixture, vol.%: Tall oil (density 950 kg / m) 24; the mother liquor (density 1095 kg / m, pH 2.3) 65; lignin (density 1060 kg / m) I. Feed rate 1570 kg / h at 90 C. Circulation speed 20 m / h.
    Analysis of separated tall oil, L:
    Tall oil 99
    Lignin1
    Mother solution
    Gypsum
    Analysis of the separated stock solution, OBL:
    Tall oil 2
    Lignin3
    Uterine Solution 95
    Gypsum
    EXAMPLE 8 The separation device of Example 4 was used in the same operations. The composition of the feed mixture, about L: tall oil (density 950 kg / me) 26; the mother liquor (density 1095 kg / m, pH 2.8) 67; lignin (density 1060 kg / m) 6. The feed rate is 2200 kg / h at 88 ° C, the circulation rate is 21 m3 / h.
    Analysis of the separated tall oil, OBL:
    Tall oil 98
    LigninI
    Uterine Solution1
    91
    Gypsum
    Analysis of the separated stock solution, vol.%:
    Tall oil 4
    Lignin2
    Royal solution 94
    Gypsum
    Example9. A water-oil mixture, obtained by mixing 490 kg / h of crude tall oil and 110 kg / h of hot water, as well as 0.4 kg / h of 100% sulfuric acid, was fed to the separator. The feed mixture has the following composition, vol.%: Gall oil (density 950 kg / me) 84; wash water (density 980 kg / m3, pH 3.2) 8; lignin 8. Feed rate of 600 kg / h at 86 ° C.
    The mixture was tangentially supplied to the mixing part 3 of the device, where the circulation rate is 20 m5 / h. The unloading of tall oil occurred over the device through the drain element-6. Wash water and lignin dispersed in it along with other impurities flowed into the exhaust pipe 12 and was discharged from the bottom of the device. The sliding pipe 13, located in the upper part of the exhaust pipe Ii2, was adjusted so that the interface between the inter-faceted oil and the washing water was at the same level as the upper edge of the mixing part.
    Analysis of the separated tall oil, vol.%:
    Tall oil 96
    Lignin3
    Wash water 1
    Gypsum
    Ash-tall oil reduction 88%.
    Example 10. The separation device of Example 9 was used in the same operations. Water-oil mixture was obtained by mixing 550 kg / h of crude tall oil and 110 kg / h of hot water, as well as 0.4 kg / h of 100% sulfuric acid.
    The feed mixture had the following composition, vol.%: Tall oil (density 950 kg / m3) 80; wash water
    (density 980 kg / m3, pH 2.3) 15; lignin 5.
    Feed rate 650 kg / h at 87 ° C. Circulation rate 20.
    Analysis of the separated washed tall oil, vol.%:
    ten
    five
    20
    five
    162
    five
    0
    five
    0
    five
    0
    ten
    Tall oil 99
    Lignin1
    Promin water
    Gypsum
    Analysis of wash water, OBL:
    Tall oil 1
    Lignin
    Wash water 98
    Gypsum1
    Tall oil ash reduction 87%.
    Example 11. The separation device of Example 9 was used in the same operations. Water-oil mixture was obtained by mixing 630 kg / h of crude tall oil and 60 kg / h of hot water, as well as 0.3 kg / h of 100% sulfuric acid. The composition of the feed mixture, vol.%: Tall oil (density 950 kg / m3) 95; wash water (density 980 kg / m, pH 1.8) 4 lignin 1. The feed rate is 690 kg / h at 88 ° C. Circulation rate 20.
    Analysis of the separated washed oil, vol.%:
    Tall oil 99
    Lignin1
     Wash water - Gypsum Analysis of separated wash water,% by volume:
    Tall oil 1
    Lignin1
    Wash water 98
    Gypsum. Reducing the ash content of tall oil 91%.
    EXAMPLE 12 The separation device of Example 9 was used in the same operations. Water-oil mixture was obtained by mixing 780 kg / h of crude tall oil and 55 kg / h of hot water, as well as 0.5 kg / h of 100% sulfuric acid.
    The feed mixture had the following composition, vol.%: Tall oil (density 950 kg / m) 93; wash water (density 980 kg / m3, pH 2.1) 4; G lignin 2; gypsum 1. A feed rate of 835 kg / h at 96 C. A circulation rate of 20 m / h.
    Analysis of separated washed tall oil, vol.%:
    Tall oil 98 Lignin1
    Wash water 1 Gypsum
    Analysis of the separated wash water, vol.%:
    Tall oil 2
    LigninI
    Wash water 96
    Gypsum I
    A decrease in tall ash content is 86%.
    Example 13 The separation device of Example 9 was used in the same operations. The water-oil mixture was obtained by mixing 1450 kg / h of crude tall oil and 44 kg / h of hot water, as well as 0.8 kg / h of 100% sulfuric acid.
    The mixture had the following composition, vol.%: Tall oil (density 950 kg / m) 95; wash water (density 980 kg / me, pH 1.5) 3; lignin 2. The feed rate is 1494 kg / h at 85 ° C. Circulation rate 20 m / h
    Analysis of the separated washed tall oil, vol.%:
    Tall oil 97
    Lignin1
    Industrial water 2
    Gypsum
    Analysis of the separated wash water, EB.%:
    Tall oil Lignin1
    Washing veda 99
    Gypsum
    A decrease in tall ash content is 89% low.
    Example 14. A separation device with a volume of m (mixing part 6.8 m, separating part 10.9 me and a lower cone 2 m) was injected into the reaction mixture obtained by stirring 7710 kg / h of light components of tall oil extracted from soda boiling liquor, 840 kg / h 93% sulfuric acid, 250 kg of steam and 2496 kg / h of water. The mixture contains about b.%; tall oil 36.4; mother liquor 62.9; lignin 0.3; gypsum 0.48.
    This mixture was passed at a speed of 1296 kg / h at 95 ° C. The mixture was passed through the fluid supply means 5 into the mixing part 3 of the device, in which a rotary motion in the volume determined by the mixing housing of the device and the cylinder 1I is located in the middle of the mixing part by means of a circulation pump 17 tangentially connected to the mixer. 3. The circulation rate is 123 m / h. Tall oil was loaded from the top of the device through the drain pipe 6, the collector 7 and the outlet 8 pipes. The mother liquor and lignin dispersed in the mixture enter the exhaust pipe 12 and are discharged through the bottom of the device. The sliding tube 13, located in the upper part of the sliding tube 12, is adjusted so that the interface between tall oil and the mother liquor is approximately at the level of the upper edge of the mixing part 3 of the device.
    Analysis of divided tall oil, about, 7,
    0 Tall oil 96.73 Lignin 0.2
    Moisture 2.9 Fiber 0.17
    The separated mother liquor contained 5, 1.98% tall oil with a density of 11–10 kg / m, pH 2.6.
    权利要求:
    Claims (2)
    [1]
    Invention Formula
    " one . A device for the continuous separation of liquid mixtures containing relatively heavy and light liquid fractions, solid impurities, including a vertically mounted vessel with a receiving bottom part, a mixture of means in the middle part of the vessel and separating parts, a liquid supply means tangentially attached to the vessel, exhaust elements for unloading light fraction, mount
    W cones in the separating part of the vessel, located one inside the other along the vertical axis at a distance from each other constituting a series of channels for easy
    5 fractions, different
    In order to increase reliability and efficiency, the mixing part is equipped with a vertically mounted cylinder at its center, having a diameter equal to 1 / 2-1 / 5 of the vessel diameter, and a circulation pump connected to it by two tangentially installed pipelines , while the distance between the cones was 550-200 mm, the angle at the apex of the cones was less than 90, and the means for unloading solid impurities had a vertical outlet element placed in the middle of the vessel, the inlet end of which is concentrically inside rtikalnogo cylinder.
    h
    [2]
    2. Method for continuous separation of tall oil from acidified soap mixture of tall oil, containing 20-55% tall oil, 45-80% stock solution with a pH of 2-3.5, 1-10% lignin and 0.3-2% suspended gypsum, characterized in that, in order to increase reliability and efficiency, a tangential supply of tall oil soap mixture to the mixing part of a vertical vessel at a speed of 1000-7000 kg / h is carried out, the said mixture is circulated during rotational movement of the flow inside mixing part of the vessel with a flow rate of
    at least 18-24 me / g, the ratio of the circulation rate to the feed rate is at least about 10 me / me with the formation of an intermediate phase containing lignin between the relatively lighter tall oil fraction and the relatively heavier uterine fraction solution, the tall oil fraction is brought into contact with several cones and the separated tall oil fraction is withdrawn, a part of the intermediate phase is directed to the mother liquor fraction, which is continuously withdrawn from the vessel at a rate ensuring minutes maintaining the intermediate phase layer not exceeding 0-0.5 m above the upper edge of the mixing portion.
    6,7.6
    S7J
    /////
    Fig 2
    ///// l
    B, 7.8
    Fiel
    6,7,8
    P
    X
    26
    类似技术:
    公开号 | 公开日 | 专利标题
    SU1574162A3|1990-06-23|Device for continuous separation of liquid mixtures and method of continuous separation of tall oil from acidified soap mixture of tall oil
    US4406789A|1983-09-27|Apparatus and installation for separating immiscible liquids with different specific gravities
    US6638437B2|2003-10-28|Multi-directional flow gravity separator
    CN102198984A|2011-09-28|Multiphase separation method and system for processing oily waste water
    US5032273A|1991-07-16|Apparatus for separating sand and oil from a waste water stream
    US4626360A|1986-12-02|Apparatus for separating sand and oil from a waste water stream
    CN102764580A|2012-11-07|White mud/ carbide slag-gypsum wet flue gas desulfurization device and method
    US8173017B2|2012-05-08|Single-cell mechanical flotation system
    US4855050A|1989-08-08|Centrifugal oil separator for removing oil from a waste flowing stream
    PL178615B1|2000-05-31|Apparatus for wet desulphurising combustion gases
    CN1261366C|2006-06-28|Integrated device for separation of oil-field production liquid and treatment of sewage
    CN102765741B|2014-04-02|Separating and purifying device and method of white mud/carbide slag-gypsum process desulphurization gypsum slurry
    CN202823268U|2013-03-27|Slurring device for white mud or acetylene sludge
    RU2135886C1|1999-08-27|Method of device for preliminary disposal of water in gathering systems of oil production wells
    KR100315903B1|2001-12-12|waste water process system used microbubble generator
    CN202754811U|2013-02-27|Separation impurity-removing device of white mud/ carbide slag-ypsum process desulfuration gypsum slurry
    SU1303556A1|1987-04-15|Device for treatment of waste water
    SU1480847A1|1989-05-23|Apparatus for jointly preparing water and oil
    CN209721702U|2019-12-03|A kind of high-load anaerobic reactor
    SU1318245A1|1987-06-23|Oil and gas separator
    SU1318975A1|1987-06-23|Flotator
    SU1152933A1|1985-04-30|Liquid purifying device
    RU2359733C1|2009-06-27|Multifunctional instrument for oil preparation
    SU1480846A1|1989-05-23|Three-phase separator
    JPH07232Y2|1995-01-11|Flotation device
    同族专利:
    公开号 | 公开日
    CA1221038A|1987-04-28|
    US4532034A|1985-07-30|
    FI66296B|1984-06-29|
    SE8400068D0|1984-01-09|
    FR2541129A1|1984-08-24|
    SE448825B|1987-03-23|
    SE8400068L|1984-07-12|
    FI66296C|1984-10-10|
    FR2541129B3|1986-12-26|
    FI830097A0|1983-01-11|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    US416048A|1889-11-26|Decanting device |
    US1030271A|1910-03-19|1912-06-25|Alexander John Arbuckle|Feed and distributing means for separators.|
    DE342265C|1921-05-03|
    US1940794A|1927-11-14|1933-12-26|Petroleum Rectifying Co California|Treated oil settling device|
    DE597301C|1932-01-24|1934-05-23|Carl Generlich|Strain tank under siphon effect|
    DE861692C|1944-07-04|1953-01-05|Metallgesellschaft Ag|Device for separating mixtures of liquids of different specific gravity|
    US2981413A|1953-11-30|1961-04-25|Dorr Oliver Inc|Process for separating solids in liquid suspension|
    FR1341018A|1962-09-28|1963-10-25|Schuechtermann & Kremer|Clarifier-thickener|
    US3250394A|1963-05-03|1966-05-10|Cities Service Athabasca Inc|Flotation apparatus|
    US3444077A|1965-01-21|1969-05-13|Harvey E Finch|Liquid clarifying method|
    SE340087B|1970-03-12|1971-11-08|Nordstjernan Rederi Ab|
    US4146471A|1975-07-21|1979-03-27|Wyness David K|Liquid clarification apparatus and method|
    SU753445A1|1977-07-25|1980-08-07|Предприятие П/Я А-7354|Apparatus for separating oil from water|
    FR2457127B1|1979-05-23|1983-09-16|Alsthom Atlantique|
    US4371382A|1980-08-06|1983-02-01|Caribbean Properties Limited|Process and apparatus for the contact and separation of immiscible fluids|
    FR2480617B1|1980-04-21|1986-01-17|Bardet Sa Ets Andre|APPARATUS AND INSTALLATION FOR SEPARATING NON-MISCIBLE LIQUIDS OF DIFFERENT DENSITIES|
    US4346005A|1981-08-03|1982-08-24|Crane Co.|Tube settler module|
    US4425239A|1981-12-24|1984-01-10|Conoco Inc.|Method and apparatus for oil-water separation|GB2158741B|1984-05-14|1988-08-17|Hydro Int Ltd|Separation of components of a fluid mixture|
    US4767536A|1987-08-27|1988-08-30|Warminster Fiberglass Company|Gas extraction outlet for wastewater settling tank|
    RU2022610C1|1988-05-20|1994-11-15|Якутский научно-исследовательский и проектный институт алмазо-добывающей промышленности|Clarification apparatus|
    US5188238A|1989-06-21|1993-02-23|Hydro International Limited|Separator for separating solids components of liquid mixtures and method of using the same|
    GB2241904B|1990-03-16|1993-12-01|Hydro Int Ltd|Separator|
    GB9023397D0|1990-10-26|1990-12-05|Tooley John K|Oil/sludge separation|
    US5143703A|1990-12-24|1992-09-01|Phillips Petroleum Company|Fluid flow control and isolation|
    US5209907A|1990-12-24|1993-05-11|Phillips Petroleum Company|Fluid flow control and isolation|
    EP1208897A1|2000-11-21|2002-05-29|Epcon Norge AS|Combined degassing and flotation tank|
    AUPR862001A0|2001-11-02|2001-11-29|Qed Corporation Limited|Apparatus for treatment of contaminated liquids|
    SE534404C2|2009-12-30|2011-08-09|Anders Goeran Hofstedt|Procedure for separating and splitting raw soap from a mixture of black liquor and raw soap|
    FI123968B|2010-02-08|2014-01-15|Upm Kymmene Corp|Process and apparatus for cleaning crude oil|
    AU2012211392B2|2011-08-29|2014-11-20|Process Group Pty Ltd|Compact Separation Apparatus|
    JP2016215106A|2015-05-18|2016-12-22|伊藤工機株式会社|Oil/water separator|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    FI830097A|FI66296C|1983-01-11|1983-01-11|CONTAINER SEPARATIONSANORDNING OCH FOERFARANDE FOER SEPARERING AV I EN VAETSKEBLANDNING INGAOENDE LAETTA OCH TUNGA VAETSKEFORMIGA FRAKTIONER|
    [返回顶部]