WO2001043846A1 - Verfahren und vorrichtung zur abtrennung von feststoffen aus einer flüssigen phase - Google Patents

Verfahren und vorrichtung zur abtrennung von feststoffen aus einer flüssigen phase Download PDF

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Publication number
WO2001043846A1
WO2001043846A1 PCT/EP2000/012665 EP0012665W WO0143846A1 WO 2001043846 A1 WO2001043846 A1 WO 2001043846A1 EP 0012665 W EP0012665 W EP 0012665W WO 0143846 A1 WO0143846 A1 WO 0143846A1
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WO
WIPO (PCT)
Prior art keywords
solid
liquid phase
liquid
sedimentation
countercurrent
Prior art date
Legal status (The legal status 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 status listed.)
Ceased
Application number
PCT/EP2000/012665
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German (de)
English (en)
French (fr)
Inventor
Michael Haubs
Reinhard Wagener
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Ticona GmbH
Original Assignee
Ticona GmbH
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 Ticona GmbH filed Critical Ticona GmbH
Priority to US10/168,269 priority Critical patent/US6818132B2/en
Priority to KR1020027007768A priority patent/KR20020055604A/ko
Priority to AT00987397T priority patent/ATE515300T1/de
Priority to CN008185506A priority patent/CN1424934B/zh
Priority to EP00987397A priority patent/EP1242154B1/de
Priority to JP2001544971A priority patent/JP4159782B2/ja
Publication of WO2001043846A1 publication Critical patent/WO2001043846A1/de
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D43/00—Separating particles from liquids, or liquids from solids, otherwise than by sedimentation or filtration
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D12/00—Displacing liquid, e.g. from wet solids or from dispersions of liquids or from solids in liquids, by means of another liquid
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B5/00—Drying solid materials or objects by processes not involving the application of heat
    • F26B5/005—Drying solid materials or objects by processes not involving the application of heat by dipping them into or mixing them with a chemical liquid, e.g. organic; chemical, e.g. organic, dewatering aids
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D11/00—Solvent extraction
    • B01D2011/002—Counter-current extraction

Definitions

  • the present invention relates to a method and an apparatus for separating solids from a liquid phase.
  • the separation of solids from a liquid phase is a common task in technology.
  • the separation of aluminum hydroxide crystals from the basic mother liquor may be mentioned as an example.
  • the process according to the invention is of particular relevance for those polymers which are prepared in a high-boiling solvent with the formation of salts or acids or bases to be neutralized subsequently.
  • Examples of such processes are the production of polyaramides from diamines and diacid chlorides, of polycarbonates from diphenols or diphenolates with phosgene, of polysulfones, polyether sulfones or polyether ketones from diphenolates and dihalogenated aromatic hydrocarbons or the production of polyarylene siloxanes from diaryl dichlorosilanes with diphenolates.
  • the term high-performance polymers includes the polyarylene sulfides.
  • poly (p-phenylene) sulfide PPS
  • the polymer In the production of poly (p-phenylene) sulfide (PPS), the polymer must be freed from high-boiling N-methylpyrrolidone (NMP) and undissolved and dissolved by-products.
  • NMP N-methylpyrrolidone
  • the proportion of residual solvent (NMP) in the Polymers should be below 100 ppm.
  • the accumulation of dilute NMP-containing wash liquors would require a great deal of distillation and must therefore be avoided.
  • the object of the present invention is to provide a method and an apparatus for the separation of solids from solid-liquid mixtures, the liquid phase being separated virtually completely from the solid without a large amount of dilute wash liquor being obtained.
  • the object of the present invention is achieved in that the solid in a first liquid phase is brought into contact with a second liquid phase in countercurrent and the solid is transferred to the second liquid phase.
  • the method according to the invention is carried out by bringing the solid in the first liquid phase in countercurrent contact with a second liquid in a device which has at least one solid-liquid inlet (1), at least one solid-liquid outlet (4) , has at least one liquid inlet (3) and at least one liquid outlet (2) (see FIG. 1 and FIG. 3).
  • the solid is placed in the first liquid phase in the solid-liquid inlet (1).
  • the second liquid phase is placed in the liquid inlet (3).
  • the solid is discharged as completely as possible in the second liquid phase from the solid-liquid outlet (4).
  • the first liquid phase is discharged as completely as possible from the liquid outlet (2).
  • the proportion of the first liquid phase, based on the second liquid phase in the solid-liquid outlet (4), is less than 50% by weight, preferably less than 10% by weight and particularly preferably less than 1% by weight ,
  • the first liquid phase is not diluted very much with the second liquid phase.
  • the proportion of the second liquid phase, based on the first liquid phase in the liquid outlet (2), is less than 80% by weight, preferably less than 50% by weight, particularly preferably less than 30% by weight.
  • This solids content based on the solids introduced into the solid-liquid inlet (1), is preferably less than 30% by weight, particularly preferably less than 10% by weight.
  • the solid passes through the device by sedimentation under gravity.
  • the solid of the solid-liquid mixture is sedimented at least once in a device and the sedimenting solid is washed with a second liquid phase in countercurrent.
  • the first liquid phase is preferably an organic solvent and the second liquid phase is water.
  • Dipolar aprotic solvents are used as organic solvents, preferably NMP.
  • the first and second liquid phases are preferably miscible.
  • the solid can consist of one or more components.
  • the main constituent of the solid is preferably a polymer such as a polyarylene sulfide, very particularly preferably PPS.
  • the method according to the invention can also separate solid mixtures from one another if its constituents dissolve differently in the first and second liquid phases. It is preferred if the main constituent of the solid dissolves neither in the first nor in the second liquid phase. Secondary components of the solid or also of the first liquid phase to be separated off preferably have good solubility in the second liquid phase.
  • a polymer to be separated and purified for example PPS
  • PPS polymer to be separated and purified
  • the contaminants to be removed for example salt and high-boiling solvent
  • Particularly advantageous in the process according to the invention is the possibility of being able to carry out the removal of the solid continuously, even under elevated temperature and pressure.
  • the density of the solid differs from the density of the first and second liquid phases.
  • the object is achieved by a method, the device of the method according to the invention containing at least one head part, at least one bottom part and at least one middle part with n sedimentation soils.
  • a first preferred embodiment of the invention is a method with a device which has at least one sedimentation base (SB) which contains at least one sedimentation funnel with a sediment outflow, at least one flow-through zone and at least one supernatant drain.
  • SB sedimentation base
  • the solid is sedimented on each sedimentation tray in the sedimentation funnel and washed in the flow zone. This process is repeated sequentially in n stages.
  • the sedimentation floor is funnel-shaped and opens into a drain that represents the solid-liquid outlet.
  • the head section contains an input for the solid-liquid mixture, which leads to the top one
  • the head section also contains an outlet for the supernatant drainage of the uppermost sedimentation soil.
  • the device of the method according to the invention makes it possible to separate the solid from the mixture in such a way that the proportion of the first liquid phase which is discharged with the solid can be reduced by increasing the number of sedimentation trays.
  • the sedimentation soils are arranged one above the other.
  • the overhang drainage of a sedimentation soil is connected to the flow zone of the following sedimentation soil above.
  • the supernatant of a sedimentation soil consists of a mixture of the first and the second liquid phase.
  • the supernatant passes through the sedimenting solid in a geometrically precisely defined arrangement and effects an at least partial displacement washing of the solid.
  • the supernatant of a sedimentation soil is used as a washing liquid for the sedimentation soil above.
  • Fresh washing liquid is fed into the flow zone of the bottom sedimentation bottom in the form of a pure second liquid phase through the liquid inlet (3). While the solid passes through the device of the method according to the invention from top to bottom, the washing liquid flows from bottom to top. This countercurrent principle achieves an extremely effective separation of the first liquid phase from the solid.
  • the geometrical arrangement of the flow zone is chosen so that the solid does not sediment directly against the inflowing washing liquid in the individual sedimentation trays.
  • the passage of the solid into the following sedimentation soil is not hindered by the washing liquid which is conducted in countercurrent, since the washing liquid is separated Supernatant leads to the flow zone of the next sedimentation floor above. This ensures largely undisturbed sedimentation, which means that solids with a low sedimentation rate can also be separated.
  • the separating effect of the device of the method according to the invention essentially depends on the number of sedimentation soils.
  • the separation effect can be adapted to the respective separation tasks by the number of sedimentation trays.
  • the separation effect increases with the number of sedimentation soils.
  • a preferred embodiment of the invention is a device with n sedimentation soils, where n is an integer from 2 to 1000.
  • a particularly preferred embodiment of the invention is a device, where n is an integer from 3 to 200.
  • a very particularly preferred embodiment of the invention is a device, where n is an integer from 4 to 100.
  • a second preferred embodiment of the invention is a method with a device which has a straight tube with a centered stirrer shaft.
  • the agitator shaft carries a cross bar stirrer with at least one level.
  • Several agitator blades or agitator bars are arranged in a horizontal plane of the cross bar agitator.
  • the geometric arrangement of the crossbar stirrer is chosen so that it largely suppress streaking of the rising liquid phase 2.
  • the impellers extend close to the inner wall of the straight one
  • the crossbar stirrer carries three to eight, particularly preferably four stirring blades or stirring bars per level.
  • the separating effect of the device of the method according to the invention essentially depends on the number and the spacing of the levels of the crossbar stirrer.
  • the separation effect can be adapted to the respective separation tasks by the number of levels.
  • the separation effect increases with the number of levels.
  • the crossbar stirrer rotates at a moderate speed during operation.
  • the speed is 0.1 to 1000 rpm, preferably 1 to 200 rpm and particularly preferably 5 to 50 rpm.
  • the uppermost sedimentation tray or the head part of the device has a larger diameter than the sedimentation trays underneath. This measure reduces the solids content in the liquid outlet (2), which forms the supernatant drain of the uppermost sedimentation soil.
  • the device can also separate very small solids.
  • the density of the solid differs from the density of the liquid phase.
  • the sedimentation rate of the solid in the liquid phase should be greater than 1 mm / min.
  • the rate of sinking of a solid depends on the density difference to the liquid phase, the average particle size, the particle size distribution and the viscosity of the liquid phase.
  • the separation performance of the device of the method according to the invention can be adapted within wide limits to the respective separation task by changing the design and setting the operating conditions.
  • the design can be changed by the number of sedimentation trays n, the inclination of the sedimentation funnel, the geometry of the sediment outflow and the projection of the protrusion, and the geometric design of the flow zone.
  • the design can be changed by the number n of the levels of the cross bar stirrer, the vertical spacing of the levels and the shape of the impeller or agitator bar.
  • Advantageous operating conditions are achieved by adjusting the inflow and outflow rates of solid-liquid mixtures, the inflow rate of the second liquid phase or the rotation speed of the crossbar stirrer.
  • Figure 1 shows an example of a first preferred embodiment of the
  • Device of the method according to the invention as a sedimentator.
  • Figure 2 shows a section (recurring unit) of the device
  • Figure 3 shows a second preferred embodiment of the device for
  • the device according to FIGS. 1 and 2 has at least one sedimentation funnel (A) with sediment outflow (D), at least one flow-through zone (B) and at least one supernatant drain (C).
  • the bottom part (BT) of the device according to FIG. 1 is funnel-shaped and opens into a drain which simultaneously represents the solid-liquid outlet (4).
  • the head part (KT) contains an input for the solid-liquid mixture (1).
  • the head part (KT) also contains a liquid outlet (2).
  • the middle section (MT) contains n sedimentation soils and a liquid inlet (3).
  • a sedimentation tray (SB) according to FIG. 2 contains a sedimentation funnel (A) with sediment outflow (D), a flow-through zone (B) and a supernatant drain (C).
  • a sedimentation funnel according to FIG. 2 consists of an inner funnel segment (A1) and an outer funnel segment (A2).
  • the inner funnel segments (A2) are attached to a rotatable inner shaft (E).
  • the device according to FIG. 3 has a straight tube (F) and a central stirring shaft (G).
  • the agitator shaft carries cross-bar stirrers arranged one above the other in several levels. Each level has four round stirring bars that extend close to the wall.
  • the bottom part (BT) of the device according to FIG. 3 is funnel-shaped and opens into a drain which represents the solid-liquid outlet (4).
  • the head part (KT) contains the liquid outlet (2) ...
  • the upper end of the tube (F) contains an inlet for the solid-liquid mixture (1).
  • the washing liquid is added via the inlet (3).
  • a test device according to FIG. 1 with a diameter of 120 mm was used.
  • the device had 20 sedimentation soils.
  • the sedimentation apparatus consists of a straight tube with a diameter of 60 mm and a length of 600 mm with a multiple cross bar stirrer, the stirring blades of which extend close to the wall.
  • the spacing of the stirring blade levels along the vertical stirring shaft is 50 mm.
  • the sedimentator with head and bottom part is shown in Figure 3.
  • the stirrer speed was set to 10 rpm.
  • 180 g per minute of a mixture of 25% by weight of polyphenylene sulfide and 5% by weight of solid sodium chloride were suspended in N-methylpyrrolidone (containing 5% by weight of water) at a temperature of 65 ° C. in the solid / liquid Input (1) given the device shown in Figure 2.
  • 110 ml per minute of water at a temperature of 65 ° C. were added to the liquid inlet (3).
  • 125 g per minute of a suspension of 45 g of polyphenylene sulfide in 80 g of water were removed from the solid-liquid outlet (4).
  • With the polyphenylene sulfide in water less than 0.2% by weight of the amount of sodium chloride introduced was discharged.
  • the NMP content of the aqueous liquid phase removed at the solid-liquid outlet was less than 0.5% by weight.
  • polyphenylene sulfide can be separated from a mixture with common salt suspended in NMP in a sedimentator without the need for highly diluted wash liquors.
  • the NMP can be without Evaporate large amounts of water completely by distillation.
  • the separation of NMP and table salt from PPS is well over 99%.
  • the process according to the invention is technically interesting due to the favorable recovery of the NMP and low loss of PPS.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • Molecular Biology (AREA)
  • Health & Medical Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • General Chemical & Material Sciences (AREA)
  • Dispersion Chemistry (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Extraction Or Liquid Replacement (AREA)
  • Separation Of Solids By Using Liquids Or Pneumatic Power (AREA)
  • Processes Of Treating Macromolecular Substances (AREA)
  • Separation Of Suspended Particles By Flocculating Agents (AREA)
  • Polymers With Sulfur, Phosphorus Or Metals In The Main Chain (AREA)
PCT/EP2000/012665 1999-12-17 2000-12-13 Verfahren und vorrichtung zur abtrennung von feststoffen aus einer flüssigen phase Ceased WO2001043846A1 (de)

Priority Applications (6)

Application Number Priority Date Filing Date Title
US10/168,269 US6818132B2 (en) 1999-12-17 2000-12-13 Method and device for separating solids from a liquid phase
KR1020027007768A KR20020055604A (ko) 1999-12-17 2000-12-13 액상으로부터 고체를 분리하는 방법 및 장치
AT00987397T ATE515300T1 (de) 1999-12-17 2000-12-13 Verfahren und vorrichtung zur abtrennung von feststoffen aus einer flüssigen phase
CN008185506A CN1424934B (zh) 1999-12-17 2000-12-13 从液相分离固体的方法和装置
EP00987397A EP1242154B1 (de) 1999-12-17 2000-12-13 Verfahren und vorrichtung zur abtrennung von feststoffen aus einer flüssigen phase
JP2001544971A JP4159782B2 (ja) 1999-12-17 2000-12-13 液相から固体を分離するための方法及び装置

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE19961143.2 1999-12-17
DE19961143 1999-12-17

Publications (1)

Publication Number Publication Date
WO2001043846A1 true WO2001043846A1 (de) 2001-06-21

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PCT/EP2000/012665 Ceased WO2001043846A1 (de) 1999-12-17 2000-12-13 Verfahren und vorrichtung zur abtrennung von feststoffen aus einer flüssigen phase

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Country Link
US (1) US6818132B2 (https=)
EP (2) EP2277612A1 (https=)
JP (2) JP4159782B2 (https=)
KR (1) KR20020055604A (https=)
CN (2) CN1424934B (https=)
AT (1) ATE515300T1 (https=)
DE (1) DE10061973A1 (https=)
WO (1) WO2001043846A1 (https=)

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WO2015047720A1 (en) 2013-09-25 2015-04-02 Ticona Llc Process for forming low halogen content polyarylene sulfides
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JP2016536377A (ja) 2013-09-25 2016-11-24 ティコナ・エルエルシー ポリアリーレンスルフィドを形成するためのスクラビングプロセス
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US9908974B2 (en) 2014-04-30 2018-03-06 Kureha Corporation Polyarylene sulfide production method and polyarylene sulfide production apparatus
WO2016133739A1 (en) 2015-02-19 2016-08-25 Ticona Llc Method for forming a high molecular weight polyarylene sulfide
WO2016133738A1 (en) 2015-02-19 2016-08-25 Ticona Llc Method for forming a low viscosity polyarylene sulfide
WO2016133740A1 (en) 2015-02-19 2016-08-25 Ticona Llc Method of polyarylene sulfide precipitation
JP6783242B2 (ja) 2015-03-25 2020-11-11 ティコナ・エルエルシー 高溶融粘度のポリアリーレンスルフィドを形成する方法
CA3014968C (en) 2017-08-18 2025-09-23 Canadian Natural Resources Limited HIGH-TEMPERATURE PARAFFINIC FOAM TREATMENT PROCESS
CN108219135B (zh) * 2017-12-25 2021-05-04 浙江新和成特种材料有限公司 一种聚苯硫醚树脂的连续洗涤装置
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CN115279734A (zh) 2019-12-20 2022-11-01 提克纳有限责任公司 形成聚芳硫醚的方法
CN117916001A (zh) 2021-09-08 2024-04-19 提克纳有限责任公司 从聚芳硫醚废污泥中回收有机溶剂的反溶剂技术
CN117916002A (zh) 2021-09-08 2024-04-19 提克纳有限责任公司 从聚芳硫醚废淤浆中回收有机溶剂的萃取技术
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US20030150804A1 (en) 2003-08-14
DE10061973A1 (de) 2001-08-09
KR20020055604A (ko) 2002-07-09
CN1424934B (zh) 2012-10-31
EP2277612A1 (de) 2011-01-26
US6818132B2 (en) 2004-11-16
JP4934109B2 (ja) 2012-05-16
JP4159782B2 (ja) 2008-10-01
EP1242154B1 (de) 2011-07-06
CN1424934A (zh) 2003-06-18
ATE515300T1 (de) 2011-07-15
JP2003516846A (ja) 2003-05-20
CN101229451A (zh) 2008-07-30
CN101229451B (zh) 2013-02-13
EP1242154A1 (de) 2002-09-25
JP2008274294A (ja) 2008-11-13

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