EP0283584B1 - Verfahren zur Verminderung des Wasser- und Aschegehalts in Rohteeren - Google Patents

Verfahren zur Verminderung des Wasser- und Aschegehalts in Rohteeren Download PDF

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Publication number
EP0283584B1
EP0283584B1 EP87118804A EP87118804A EP0283584B1 EP 0283584 B1 EP0283584 B1 EP 0283584B1 EP 87118804 A EP87118804 A EP 87118804A EP 87118804 A EP87118804 A EP 87118804A EP 0283584 B1 EP0283584 B1 EP 0283584B1
Authority
EP
European Patent Office
Prior art keywords
phase
tar
water
process according
crude
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.)
Expired - Lifetime
Application number
EP87118804A
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German (de)
English (en)
French (fr)
Other versions
EP0283584A1 (de
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.)
Ruetgers 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/de
Application granted granted Critical
Publication of EP0283584B1 publication Critical patent/EP0283584B1/de
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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 approximately 15 bar under gravity leads to a reduction in the water content. 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.
  • FR-A 2 336 471 it is proposed to heat up the tar flowing out of the gravity separator with water contents up to 20% via a steam-heated heat exchanger during the coke oven gas processing and to feed it to a three-phase decanter centrifuge in order to separate it into the three phases water, tar and thick tar (see also: Petroleum and Coal, 1977, pp. 558 to 564). Residual water contents of generally less than 5% are achieved. The raw tar obtained in this way is stable in storage and ready for sale. Information on the degrees of clarification achieved is given in the Publication as little as indications of the tar content of the aqueous phase. However, since the water is returned to the gravity separator for clarification according to the process scheme, it can be assumed that the water contains not only soluble tar substances but also considerable amounts of undissolved substances.
  • 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, fluctuations in the composition of the raw tars play no role. 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 task was therefore to develop a continuous process for reducing the content of water and ash formers in pre-cleaned hard coal tars, in which, despite sufficient separation and clarification levels, the demands for low sedimentation time and low losses of ash-free QI are met.
  • 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 times gravitational acceleration (g), which is provided with an open single or double-start, preferably armored screw and the usual weirs and discharge devices 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 of 10 to 50 min- 1 is continuously divided into an aqueous, a tar and a solid phase, during which continuous operation, the feed is periodically interrupted briefly.
  • gravitational acceleration g
  • 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:
  • a raw tar stored at 60 ° C is heated to 85 ° C and fed in an amount of 4.0 m 3 / 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 every 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 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 Verfahren zur Verminderung des Wasser- und Aschegehalts in Rohteeren Expired - Lifetime EP0283584B1 (de)

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 EP0283584A1 (de) 1988-09-28
EP0283584B1 true EP0283584B1 (de) 1990-08-29

Family

ID=6323771

Family Applications (1)

Application Number Title Priority Date Filing Date
EP87118804A Expired - Lifetime EP0283584B1 (de) 1987-03-23 1987-12-18 Verfahren zur Verminderung des Wasser- und Aschegehalts in Rohteeren

Country Status (6)

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

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102015112532A1 (de) 2015-06-08 2016-12-08 L'Air Liquide, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Verfahren zur Wäsche organischer Flüssigkeiten

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2002102938A1 (en) * 2001-06-18 2002-12-27 Sasol Technology (Pty) Ltd Method of separating particles from a hydrocarbon composition
US10947469B2 (en) * 2019-05-13 2021-03-16 James Chun Koh Apparatus and method for manufacturing bio emulsion fuel using vegetable oil

Family Cites Families (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
DE2558857A1 (de) * 1975-12-27 1977-07-14 Otto & Co Gmbh Dr C Verfahren zur verarbeitung der bei verkokungsoefen anfallenden spuelfluessigkeit der gasvorlage
DE2707111C3 (de) * 1977-02-18 1979-08-23 Flottweg-Werk Dr. Georg Bruckmayer Gmbh & Co Kg, 8313 Vilsbiburg Vollmantel-Schneckenzentrifuge zur Trennung eines Feststoff-Flüssigkeitsgemisches
AT387160B (de) * 1984-08-30 1988-12-12 Voest Alpine Ag Zentrifuge fuer die entwaesserung und trocknung vorentwaesserter schlaemme

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102015112532A1 (de) 2015-06-08 2016-12-08 L'Air Liquide, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Verfahren zur Wäsche organischer Flüssigkeiten

Also Published As

Publication number Publication date
ES2003848B3 (es) 1991-03-01
PL151440B1 (en) 1990-09-28
CS273648B2 (en) 1991-03-12
CS83788A2 (en) 1990-08-14
PL271346A1 (en) 1989-02-06
DE3764637D1 (de) 1990-10-04
EP0283584A1 (de) 1988-09-28
DE3709465A1 (de) 1988-10-06
JPS63254187A (ja) 1988-10-20
ES2003848A4 (es) 1988-12-01

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