EP0283584A1 - Procédé de diminution de la teneur en eau et en cendres des groudrons bruts - Google Patents

Procédé de diminution de la teneur en eau et en cendres des groudrons bruts Download PDF

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Publication number
EP0283584A1
EP0283584A1 EP87118804A EP87118804A EP0283584A1 EP 0283584 A1 EP0283584 A1 EP 0283584A1 EP 87118804 A EP87118804 A EP 87118804A EP 87118804 A EP87118804 A EP 87118804A EP 0283584 A1 EP0283584 A1 EP 0283584A1
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EP
European Patent Office
Prior art keywords
tar
phase
water
raw
content
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.)
Granted
Application number
EP87118804A
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German (de)
English (en)
Other versions
EP0283584B1 (fr
Inventor
Gerd-Peter Dr. Blümer
Reinhard Alff
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.)
Rain Carbon Germany GmbH
Original Assignee
Ruetgerswerke AG
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 Ruetgerswerke AG filed Critical Ruetgerswerke AG
Publication of EP0283584A1 publication Critical patent/EP0283584A1/fr
Application granted granted Critical
Publication of EP0283584B1 publication Critical patent/EP0283584B1/fr
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10C—WORKING-UP PITCH, ASPHALT, BITUMEN, TAR; PYROLIGNEOUS ACID
    • C10C1/00—Working-up tar
    • C10C1/02—Removal of water

Definitions

  • the invention relates to a mechanical method for reducing the content of water and ash formers in hard coal tars by means of centrifuges.
  • Water is most often separated by decanting under gravity at 60 ° C.
  • the water content can be reduced to about 3%.
  • Pressure drainage at temperatures up to 200 ° C and pressures of about 15 bar under gravity leads to a reduction in the water content to about 1 to 1.5%.
  • pressure-resistant retorts are required for this. This limits the applicability to small amounts of tar.
  • the plate separators proposed for cleaning the raw tars with continuous solids discharge via nozzles are highly solids-oriented. They are therefore designed for the maximum solids concentration that occurs. If the solids content in the inlet decreases, the concentration in the discharge must also decrease accordingly. Since the solids must be flowable, solids concentrations of only about 60% can be achieved in the discharge. If the concentration drops from 5 to 0.5% in the inlet, it drops to around 6% in the outlet.
  • the plate packs of the separators are provided with risers that should lie in the level of the separating layer between the light (water) and heavy phase (tar) so that an optimal separation is guaranteed. Since the position of the separating layer depends on the density ratio between tar and water, it shifts when the density of the tar changes.
  • the only goal could have been to prevent sedimentation during storage.
  • only the relatively coarse solids consisting of coke and ash dust are removed.
  • the aim of the proposed method using a three-phase decanter centrifuge is thus a raw tar pre-cleaning, in which fluctuations in the composition are compensated for by the storage in the downstream storage containers.
  • the sedimentation time should not be less than 10 minutes if sufficient degrees of separation and clarification were to be achieved. Since the process is carried out discontinuously, play Fluctuations in the composition of the raw teas do not matter. There is also no mixing of the phases caused by an additional flow, as in continuous processes. The results are therefore not transferable to continuous processes, the results of which, as expected, must be significantly worse under comparable conditions. However, the long sedimentation times show that the proposed method is not very suitable for industrial implementation.
  • the object is achieved in that the optionally pretreated raw tar in a three-phase decanter centrifuge with a centrifugal number between 1000 and 3000.
  • a centrifugal number between 1000 and 3000.
  • g which is provided with an open one or two-flight, preferably armored screw and the usual weirs and discharge devices, at a temperature between 60 and 105 ° C, an average residence time of the tar between 30 and 80 s and a differential speed between the screw and rotor from 10 to 50 min ⁇ 1 is continuously divided into an aqueous, a tar and a solid phase, with the feed being periodically interrupted briefly during continuous operation.
  • the raw tars can be treated with demulsifiers, flocculants and / or diluents before decanting, as is common in separation technology to improve the degree of clarification or separation. Decanting can also be preceded by water washing, as is customary in the tar industry to reduce the salt content.
  • Decanters are generally used for the clarification of liquids whose solids content is so high that they can no longer be processed in plate separators.
  • the usual solids content is between 20 and 60%.
  • Such solids contents can be achieved in coke oven gas processing in coke oven plants with filling gas extraction.
  • example 1 the dewatering and ash removal of the tar is carried out in a conventional three-phase decanter centrifuge, as suggested by Ullrich and Loss. The results of this comparison test thus characterize the state of the art.
  • example 2 the decanter modified in the manner according to the invention is used without the method being changed compared to example 1. Examples 3 and 4 show two variants of the claimed method.
  • a raw tar stored at 60 ° C is heated to 80 ° C by means of a temperature-controlled steam heating and fed in a quantity of 3.8 m3 / h to a cylindrical three-phase decanter centrifuge with conical discharge.
  • the centrifuge is characterized by the following parameters: Drum length: 1260 mm Drum diameter: 355 mm Drum speed: 3600 min ⁇ 1 Spin number: 2550 g Differential speed: 30 min ⁇ 1 Layer thickness of the phase: Water: 41 mm Tar: 8 mm Solid: 2 mm Weir height for the tar phase: 42.5 mm Full screw, single-start, pitch: 114 mm
  • a raw tar stored at 60 ° C is heated to 85 ° C and fed in an amount of 4.0 m3 / h to the same three-phase decanter as in Example 1.
  • the centrifuge is equipped with a single-start open helical screw (pitch 114 mm, helix height 30 mm, corresponding to approximately 3/5 of the total thickness of all phases).
  • Example 2 is repeated with a raw tar temperature of 82 ° C., the feed into the three-phase decanter centrifuge being interrupted at intervals of 4 hours for a period of 1 min.
  • This example comprises 5 test series with different pretreated raw tars.
  • the raw tar temperatures and throughput are also varied.
  • the raw tars are in a tank at 60 ° C 5 vol .-% of a tar fraction boiling between 200 and 230 ° C, 0.1 vol .-% of a commercially available demulsifier and 5 vol .-% water (test series a to c) or 10 Vol .-% of a 50% tar / water emulsion added.
  • the contents are mixed by pumping over the entire duration of the experiment.
  • the insert for the decanter centrifuge is removed approximately in the middle of the tank, at the same time a corresponding raw tar, tar oil, demulsifier and water or emulsion quantity are fed into the tank.
  • the tar oil additive is said to reduce the viscosity of the raw tar and the demulsifier to break the tar / ash / water emulsion in order to achieve a better separation.
  • the additional water is said to dissolve salts from the raw tar in order to reduce the chlorine content.
  • the water and the solids are separated off in the same way with the same decanter centrifuge as in Example 3.
  • the sample is taken 22 hours after the start of the test.
  • the solid phase is completely free of water, so that it is e.g. B. in a two-phase decanter centrifuge can be concentrated in a simple manner to the extent that a free-flowing carbon concentrate remains, which can be used as a mixture component for hard coal.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Materials Engineering (AREA)
  • Organic Chemistry (AREA)
  • Centrifugal Separators (AREA)
  • Solid Fuels And Fuel-Associated Substances (AREA)
  • Processing Of Solid Wastes (AREA)
EP87118804A 1987-03-23 1987-12-18 Procédé de diminution de la teneur en eau et en cendres des groudrons bruts Expired - Lifetime EP0283584B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE19873709465 DE3709465A1 (de) 1987-03-23 1987-03-23 Verfahren zur verminderung des wasser- und aschegehalts in rohteeren
DE3709465 1987-03-23

Publications (2)

Publication Number Publication Date
EP0283584A1 true EP0283584A1 (fr) 1988-09-28
EP0283584B1 EP0283584B1 (fr) 1990-08-29

Family

ID=6323771

Family Applications (1)

Application Number Title Priority Date Filing Date
EP87118804A Expired - Lifetime EP0283584B1 (fr) 1987-03-23 1987-12-18 Procédé de diminution de la teneur en eau et en cendres des groudrons bruts

Country Status (6)

Country Link
EP (1) EP0283584B1 (fr)
JP (1) JPS63254187A (fr)
CS (1) CS273648B2 (fr)
DE (2) DE3709465A1 (fr)
ES (1) ES2003848B3 (fr)
PL (1) PL151440B1 (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2002102938A1 (fr) * 2001-06-18 2002-12-27 Sasol Technology (Pty) Ltd Procede de separation de particules a partir d'une composition d'hydrocarbures

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
RU2196800C1 (ru) * 2001-08-13 2003-01-20 Казанское открытое акционерное общество "Органический синтез" Способ обработки и утилизации тяжелой пиролизной смолы
RU2223299C2 (ru) * 2002-02-21 2004-02-10 Казанское открытое акционерное общество "Органический синтез" Способ подготовки и утилизации тяжелой пиролизной смолы
EP3103858A1 (fr) 2015-06-08 2016-12-14 L'Air Liquide Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Procede de lavage de liquides organiques avec une solution comprenant des composés fluorohydrocarbonés
US10947469B2 (en) * 2019-05-13 2021-03-16 James Chun Koh Apparatus and method for manufacturing bio emulsion fuel using vegetable oil

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE574358C (de) * 1930-11-30 1933-04-12 Hans Just Dr Ing Verfahren zur Herstellung von praktisch aschefreien Teeren
FR2336471A1 (fr) * 1975-12-27 1977-07-22 Otto & Co Gmbh Dr C Procede pour le traitement du liquide d'irrigation du barillet de fours a coke
FR2380819A1 (fr) * 1977-02-18 1978-09-15 Flottweg Werk Bruckmayer Centrifugeuse a vis sans fin, a enveloppe pleine, pour la separation d'un melange de matiere solide et de liquide
EP0173676A1 (fr) * 1984-08-30 1986-03-05 VOEST-ALPINE Aktiengesellschaft Centrifugeuse pour la déshydratation et le séchage de boues déshydratées au préalable

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE574358C (de) * 1930-11-30 1933-04-12 Hans Just Dr Ing Verfahren zur Herstellung von praktisch aschefreien Teeren
FR2336471A1 (fr) * 1975-12-27 1977-07-22 Otto & Co Gmbh Dr C Procede pour le traitement du liquide d'irrigation du barillet de fours a coke
FR2380819A1 (fr) * 1977-02-18 1978-09-15 Flottweg Werk Bruckmayer Centrifugeuse a vis sans fin, a enveloppe pleine, pour la separation d'un melange de matiere solide et de liquide
EP0173676A1 (fr) * 1984-08-30 1986-03-05 VOEST-ALPINE Aktiengesellschaft Centrifugeuse pour la déshydratation et le séchage de boues déshydratées au préalable

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2002102938A1 (fr) * 2001-06-18 2002-12-27 Sasol Technology (Pty) Ltd Procede de separation de particules a partir d'une composition d'hydrocarbures

Also Published As

Publication number Publication date
CS83788A2 (en) 1990-08-14
JPS63254187A (ja) 1988-10-20
DE3764637D1 (de) 1990-10-04
PL151440B1 (en) 1990-09-28
CS273648B2 (en) 1991-03-12
ES2003848B3 (es) 1991-03-01
PL271346A1 (en) 1989-02-06
EP0283584B1 (fr) 1990-08-29
ES2003848A4 (es) 1988-12-01
DE3709465A1 (de) 1988-10-06

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