EP0221061A1 - Method for the separation of water obtained form a coking process into a small high salt content fraction and a large low salt content fraction. - Google Patents

Method for the separation of water obtained form a coking process into a small high salt content fraction and a large low salt content fraction.

Info

Publication number
EP0221061A1
EP0221061A1 EP85902990A EP85902990A EP0221061A1 EP 0221061 A1 EP0221061 A1 EP 0221061A1 EP 85902990 A EP85902990 A EP 85902990A EP 85902990 A EP85902990 A EP 85902990A EP 0221061 A1 EP0221061 A1 EP 0221061A1
Authority
EP
European Patent Office
Prior art keywords
salt
salt content
fraction
condensate
content fraction
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
EP85902990A
Other languages
German (de)
French (fr)
Other versions
EP0221061B1 (en
Inventor
Georg Pollert
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.)
Bergwerksverband GmbH
Original Assignee
Bergwerksverband 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 Bergwerksverband GmbH filed Critical Bergwerksverband GmbH
Publication of EP0221061A1 publication Critical patent/EP0221061A1/en
Application granted granted Critical
Publication of EP0221061B1 publication Critical patent/EP0221061B1/en
Expired legal-status Critical Current

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/04—Purifying combustible gases containing carbon monoxide by cooling to condense non-gaseous materials
    • C10K1/06—Purifying combustible gases containing carbon monoxide by cooling to condense non-gaseous materials combined with spraying with water
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/001—Purifying combustible gases containing carbon monoxide working-up the condensates

Definitions

  • the invention relates to a method for separating the coal water obtained in the coking process into a small salt-rich and a large salt-poor fraction according to the preamble of claim 1.
  • the approximately 80 ° C hot gas coming from the riser pipe is cooled in the receiver by means of circulated gas condensates to the dew point at approximately 80 ° C. Only a part of the fixed salts get into the circulating condensate, the rest goes with the gas into the cooler condensates, so that a division of the gas condensates into a salt-containing and a salt-free fraction is not possible.
  • the invention is therefore based on the object to remove the fixed salts not deposited during the template spraying before the gas condensation in the precoolers from the gas, so that the majority of the water obtained in the coking is salt-free and after further cleaning steps as process water in the To be able to reduce coke oven operations.
  • the invention will be described in more detail with reference to the drawing.
  • the figure shows schematically the gas cleaning after the coke ovens.
  • the circulation of the tar and water condensed in the template 1 takes place via line 2 to the tar separator 3 and further via line 4 back to the template 1.
  • the gas flow enters the precooler 6 from the template 1 through the electrostatic filter 5.
  • the outflow of the electrostatic filter 5 is conducted via line 7 into the template circuit, for example into the tar separator 3.
  • a condensate is obtained in the pre-coolers 6, which is practically free of fixed salts and is further processed separately.
  • Part of the precooler condensate is fed via line 8 into the receiver circuit, e.g. as shown here, returned to the template 1, since in addition to the coal water, the water vapor is condensed out, which was previously evaporated in the template 1 to cool the hot raw gas.
  • the amount of water drawn off from the supply circuit through line 9 can, for example, be freed from its volatile pollutants in a stripper and, with the addition of lime, sodium hydroxide solution or sodium carbonate, also from fixed ammonia and removed after de-phenolization. Since this is a comparatively small amount of water, this solution can also be evaporated to recover the fixed salts as a solid.
  • the condensate obtained in the pre-coolers is freed of its volatile pollutants, if necessary after use in gas cleaning, and can be used after further biological cleaning, reverse osmosis, after de-phenolization or cleaning with activated carbon as process water, e.g. for coke quenching or as cooling water , used in the coking plant.
  • naphthalene deposits can occur in the precoolers 6 in the method according to the invention, fractional condensation of the gases is carried out in a number of precoolers 6 according to one embodiment of the invention.
  • the gas in the first cooler is only cooled to such an extent that the condensed (at about 70 ° C) amount of water can be used as process water.
  • a second cooler is sprinkled with tar or a tar-ammonia / water mixture to prevent naphthalene deposits.
  • the outlet of the second cooler is then fed through line 8 into the template circuit, e.g. returned to template 1, 1.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Electrostatic Separation (AREA)
  • Industrial Gases (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)

Abstract

Dans le but de séparer l'eau obtenue dans un processus de cokéfaction dans une petite fraction à haute concentration de sel et dans une grande fraction pauvre en sel, on refroidit le gaz brut dans le barillet et on le conduit à travers un filtre électrique, avant d'entrer dans le prérefroidisseur. Le condensat du barillet et l'écoulement de l'électrofiltre sont conduits dans le séparateur de goudron, tandis que le condensat du prérefroidisseur n'est qu'en partie réintroduit dans le circuit du barillet et on obtient un résidu pauvre en sel. Par contre, la phase aqueuse du séparateur de goudron est traitée en partie comme fraction riche en sel; après la sortie du filtre électrique, le gaz brut peut être fractionné dans plusieurs prérefroidisseurs.In order to separate the water obtained in a coking process in a small fraction with a high concentration of salt and in a large fraction low in salt, the raw gas in the barrel is cooled and it is led through an electric filter, before entering the precooler. The condensate from the barrel and the flow from the electrostatic precipitator are led into the tar separator, while the condensate from the precooler is only partially reintroduced into the barrel circuit and a low-salt residue is obtained. On the other hand, the aqueous phase of the tar separator is partially treated as a fraction rich in salt; after the outlet of the electric filter, the raw gas can be fractionated in several precoolers.

Description

Verfahren zur Auftrennung des beim Verkoküngsprozeß anfallenden Wassers in eine kleine salzreiche und eine große salzarme FraktionProcess for separating the water from the coking process into a small salt-rich and a large salt-poor fraction
Die Erfindung betrifft ein Verfahren zur Auftrennung des beim Verkokungsprozeß anfallenden Kohlewassers in eine kleine salzreiche und eine große salzarme Fraktion gemäß dem Oberbegriff des Anspruchs 1.The invention relates to a method for separating the coal water obtained in the coking process into a small salt-rich and a large salt-poor fraction according to the preamble of claim 1.
Bei der Verkokung von Kohle fallen im allgemeinen pro Tonne Kohle 140 1 Kohlewasser an, die zu etwa 100 1 aus der ursprünglichen Kohlenfeuchte stammen und zu etwa 40 1 sich bei der Verkokung gebildet haben. Außerdem werden bei der Verkokung neben flüchtigen Schadstoffen, wie beispielsweise NH3, H2S und HCN, auch sogenannte fixe Salze, wie hauptsächlich z.B. NH4Cl gebildet, die sich im Gaskondensat lösen und durch desorptive Prozesse nicht daraus wieder entfernt werden können. Daher ist es bisher nicht möglich, das nach Reinigungsstufen, wie beispielsweise Entphenolung oder Strippen im Abtreiber, anfallende Gaskondensat wieder als Brauchwasser zu verwenden, weil seine Salzfracht auch nach dem Entbinden des fixen Ammoniaks mit Kalk oder Alkali unverändert hoch bleibt.When coking coal, 140 l of coal water are generally produced per ton of coal, about 100 l of which originate from the original coal moisture and about 40 l have formed during the coking. In addition to volatile pollutants such as NH 3 , H 2 S and HCN, so-called fixed salts, such as mainly NH 4 Cl, are formed during coking, which dissolve in the gas condensate and cannot be removed from it again by desorptive processes. Therefore, it has not been possible to use the gas condensate after cleaning stages, such as de-phenolization or stripping in the stripper, as service water, because its salt load remains unchanged even after the fixed ammonia has been released with lime or alkali.
Üblicherweise wird auf der Kokerei das aus dem Steigrohr kommende, etwa 80ºC heiße Gas in der Vorlage durch im Kreislauf geführte Gaskondensate bis zum Taupunkt bei etwa 80°C abgekühlt. Dabei gelangen die fixen Salze nur zu einem Teil in das Kreislaufkondensat, der Rest gelangt mit dem Gas in die Kühlerkondensate, so daß eine Aufteilung der Gaskondensate in eine salzhaltige und ein salzfreie Fraktion nicht möglich ist.Usually, the approximately 80 ° C hot gas coming from the riser pipe is cooled in the receiver by means of circulated gas condensates to the dew point at approximately 80 ° C. Only a part of the fixed salts get into the circulating condensate, the rest goes with the gas into the cooler condensates, so that a division of the gas condensates into a salt-containing and a salt-free fraction is not possible.
Es ist zwar ein Verfahren zur Gewinnung eines an fixen Salzen freien Kondensats bekannt, bei dem das Rohgas zwischen Vorlage und Vorkühlern gewaschen wird, um die fixen Salze aus dem Gas abzuscheiden (US-PS 1 747 616). Eine Untersuchung dieser aus dem Jahre 1922 stammenden Arbeitsweise zeigte jedoch, daß diese Arbeitsweise keinen Erfolg hat, da die fixen Salze in Form von Aerosolen vorliegen, die in einem Waschprozeß nicht abgeschieden werden können.A method for obtaining a condensate free of fixed salts is known, in which the raw gas is washed between the receiver and precoolers in order to separate the fixed salts from the gas (US Pat. No. 1,747,616). However, an examination of this method, which dates from 1922, showed that this method was unsuccessful, since the fixed salts are in the form of aerosols, which cannot be separated in a washing process.
Der Erfindung liegt deshalb die Aufgabe zugrunde, die bei der Vorlagenbedüsung nicht abgeschiedenen fixen Salze vor der Gaskondensation in den Vorkühlern aus dem Gas zu entfernen, um so den größsten Teil des bei der Verkokung anfallenden Wassers salzfrei zu gewinnen und nach weiteren Reinigungsschritten als Brauchwasser in den Kokereibetrieb zurückführen zu können.The invention is therefore based on the object to remove the fixed salts not deposited during the template spraying before the gas condensation in the precoolers from the gas, so that the majority of the water obtained in the coking is salt-free and after further cleaning steps as process water in the To be able to reduce coke oven operations.
Diese Aufgabe wird durch ein Verfahren mit den Merkmalen gemäß dem Anspruch 1 gelöst. Weitere Ausgestaltungen und Verbesserungen erfolgen gemäß den Merkmalen der Unteransprüche.This object is achieved by a method with the features according to claim 1. Further refinements and improvements are made in accordance with the features of the subclaims.
Indem man die Kokereirohgase zwischen Vorlage und Vorkühlern ein Elektrofilter passieren läßt, werden die fixen Salze zu über 96 % aus dem wasserdampfgesättigten Rohgas abgeschieden.By letting the raw coke oven gases pass through an electrostatic precipitator between the receiver and pre-coolers, over 96% of the fixed salts are separated from the raw gas saturated with water vapor.
Anhand der Zeichnung sei die Erfindung näher beschrieben. Die Figur stellt schematisch die Gasreinigung nach den Koksöfen dar. Der Kreislauf des in der Vorlage 1 kondensierten Teers und Wassers erfolgt über Leitung 2 zum Teerscheider 3 und weiter über Leitung 4 zurück zur Vorlage 1. Der Gasström tritt dagegen aus der Vorlage 1 durch das Elektrofilter 5 in die Vorkühler 6 ein. Der Ablauf des Elektrofilters 5 wird über Leitung 7 in den Vorlagenkreislauf, beispielsweise in den Teerscheider 3, geführt. In den Vorkühlern 6 wird ein Kondensat gewonnen, das praktisch frei von fixen Salzen ist und getrennt weiterbehandelt wird.The invention will be described in more detail with reference to the drawing. The figure shows schematically the gas cleaning after the coke ovens. The circulation of the tar and water condensed in the template 1 takes place via line 2 to the tar separator 3 and further via line 4 back to the template 1. The gas flow, however, enters the precooler 6 from the template 1 through the electrostatic filter 5. The outflow of the electrostatic filter 5 is conducted via line 7 into the template circuit, for example into the tar separator 3. A condensate is obtained in the pre-coolers 6, which is practically free of fixed salts and is further processed separately.
Ein Teil der Vorkühlerkondensate wird über Leitung 8 in den Vorlagenkreislauf, z.B. wie hier dargestellt, in die Vorlage 1, zurückgeführt, da neben dem Kohlewasser auch der Wasserdampf auskondensiert wird, der vorher in der Vorlage 1 zum Kühlen des heißen Rohgases verdampft worden ist.Part of the precooler condensate is fed via line 8 into the receiver circuit, e.g. as shown here, returned to the template 1, since in addition to the coal water, the water vapor is condensed out, which was previously evaporated in the template 1 to cool the hot raw gas.
Bei dieser Arbeitsweise kommt es jedoch zu einer Anreicherung der fixen Salze im Vorlagenkreislauf, die zu Schwierigkeiten bei der Teerabscheidung führen kann. Deshalb wird kontinuierlich durch Leitung 9 eine dem Anreicherungsgrad entsprechende Flüssigkeitsmenge aus dem Vσrlagenkreislauf abgezogen. Diese Menge wird durch zusätzlich durch Leitung 8 zurückgeführtes Kühlerkondensat ausgeglichen.In this way of working, however, the fixed salts accumulate in the supply circuit, which can lead to difficulties in tar separation. Therefore, a quantity of liquid corresponding to the degree of enrichment is continuously withdrawn from the reservoir circuit through line 9. This amount is compensated for by additional cooler condensate returned through line 8.
Die durch Leitung 9 aus dem Vorlagenkreislauf abgezogene Wassermenge kann beispielsweise in einem Abtreiber von ihren flüchtigen Schadstoffen und bei Zugabe von Kalk, Natronlauge oder Natriumkarbonat auch von fixem Ammoniak befreit und nach einer Entphenolung abgeleitet werden. Da es sich um eine vergleichsweise geringe Wassermenge handelt, kann diese Lösung auch eingedampft werden, um die fixen Salze als Feststoff zu gewineen. Das in den Vorkühlern gewonnene Kondensat wird, gegebenenfalls nach einer Verwendung in der Gasreinigung, von seinen flüchtigen Schadstoffen befreit und kann nach einer weitergehenden biologischen Reinigung, einer umgekehrten Osmose, nach einer Entphenolung oder einer Reinigung mit Aktivkohle als Brauchwasser, beispielsweise zum Kokslöschen oder als Kühlwasser, in der Kokerei verwendet werden.The amount of water drawn off from the supply circuit through line 9 can, for example, be freed from its volatile pollutants in a stripper and, with the addition of lime, sodium hydroxide solution or sodium carbonate, also from fixed ammonia and removed after de-phenolization. Since this is a comparatively small amount of water, this solution can also be evaporated to recover the fixed salts as a solid. The condensate obtained in the pre-coolers is freed of its volatile pollutants, if necessary after use in gas cleaning, and can be used after further biological cleaning, reverse osmosis, after de-phenolization or cleaning with activated carbon as process water, e.g. for coke quenching or as cooling water , used in the coking plant.
Da es beim erfindungsgemäßen Verfahren zu Naphthalinablagerungen in den Vorkühlern 6 kommen kann, wird nach einer Ausführungsform der Erfindung eine fraktionierende Kondensation der Gase in mehreren Vorkühlern 6 durchgeführt. Dabei wird das Gas im ersten Kühler nur soweit abgekühlt, daß die auskondensierte (bei etwa 70ºC) Wassermenge als Brauchwasser genutzt werden kann. Bei der Kühlung auf Umgebungstemperatur wird ein zweiter Kühler mit Teer oder einem Teer-Ammoniak- wassergemisch berieselt, um Naphthalinablagerungen zu vermeiden. Der Ablauf des zweiten Kühlers wird dann durch Leitung 8 in den Vorlagenkreislauf, z.B. in die Vorlage 1, 1zurückgeführt.Since naphthalene deposits can occur in the precoolers 6 in the method according to the invention, fractional condensation of the gases is carried out in a number of precoolers 6 according to one embodiment of the invention. The gas in the first cooler is only cooled to such an extent that the condensed (at about 70 ° C) amount of water can be used as process water. When cooling to ambient temperature, a second cooler is sprinkled with tar or a tar-ammonia / water mixture to prevent naphthalene deposits. The outlet of the second cooler is then fed through line 8 into the template circuit, e.g. returned to template 1, 1.
Die folgende Tabelle zeigt die Wirkung des erfindungsgemäßen Elektrofilters auf die Gaszusammensetzung zwischen Vorlage 1 und Vorkühlern 6.The following table shows the effect of the electrostatic filter according to the invention on the gas composition between receiver 1 and precooler 6.
Rohgaszusammensetzung ohne und nach einem Elektrofilter mit den folgenden technischen Daten: Höhe: 6,5 m; Durchmesser: 1,08 m; Unterteilung in 55 Waben; Gasdurchsatz: 1.000 m3 i.N./h; Gleichspannung: 57 KV's vor (ohne) hinter E-Filter E-FilterRaw gas composition without and after an electrostatic precipitator with the following technical data: Height: 6.5 m; Diameter: 1.08 m; Divided into 55 honeycombs; Gas flow: 1,000 m 3 iN / h; DC voltage: 57 KV's before (without) after E-Filter E-Filter
Gastemperatur ºC 82 81 Teer über C10H8 g/ /m3 78,1 14,8Gas temperature ºC 82 81 tar above C 10 H 8 g / / m 3 78.1 14.8
H2O g/m3 811,0 765,0 NH3 g/m3 18,6 16,9H 2 O g / m 3 811.0 765.0 NH 3 g / m 3 18.6 16.9
H2S g/m3 13,8 13,7CC6H6 g/m3 43,5 37,8 C1 g/m3 1,6 0,06 H 2 S g / m 3 13.8 13.7 C C 6 H 6 g / m 3 43.5 37.8 C1 g / m 3 1.6 0.06

Claims

Patentansprüche Claims
1. Verfahren zur Auftrennung des beim Verkokungsprozeß während der Kühlung des heißen Rohgases in der Vorlage und den Vorkühlern anfallenden Wassers in eine kleine salzreiche und eine große salzarme Fraktion, dadurch gekennzeichnet, daß a) das Rohgas nach der Kühlung in der Vorlage zunächst durch ein Elektrofilter geführt wird, bevor es zur weiteren Kühlung in die Vorkühler eintritt, b) das Vorlagenkondensat und der Elektrofilterablauf im Teerscheider zusammengeführt werden, c) das Vorkühlerkondensat teilweise in den Vorlagenkreislauf zurückgeführt wird, während der Rest als salzarme Fraktion weiterbehandelt wird und d) die wäßrige Phase des Teerscheiders teilweise als salzreiche Fraktion weiterbehandelt wird.1. A process for separating the coking process during the cooling of the hot raw gas in the receiver and the precoolers water into a small salt-rich and a large salt-poor fraction, characterized in that a) the raw gas after cooling in the receiver first by an electrostatic filter is conducted before it enters the precooler for further cooling, b) the receiver condensate and the electrostatic filter drain are brought together in the tar separator, c) the precooler condensate is partially returned to the receiver circuit, while the rest is further treated as a low-salt fraction, and d) the aqueous phase of the tar separator is partially treated as a salt-rich fraction.
2. Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß das Rohgas nach dem Austritt aus einem Elektrofilter in mehreren Vorkühlern fraktioniert gekühlt wird. 2. The method according to claim 1, characterized in that the raw gas is fractionally cooled in several precoolers after exiting an electrostatic filter.
EP85902990A 1984-06-28 1985-06-19 Method for the separation of water obtained form a coking process into a small high salt content fraction and a large low salt content fraction Expired EP0221061B1 (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE19843423798 DE3423798A1 (en) 1984-06-28 1984-06-28 METHOD FOR SEPARATING THE WATER RESULTING FROM THE COCING PROCESS INTO A SMALL SALT-HIGH AND A LARGE SALT-LOW FRACTION
DE3423798 1984-06-28

Publications (2)

Publication Number Publication Date
EP0221061A1 true EP0221061A1 (en) 1987-05-13
EP0221061B1 EP0221061B1 (en) 1988-10-12

Family

ID=6239344

Family Applications (1)

Application Number Title Priority Date Filing Date
EP85902990A Expired EP0221061B1 (en) 1984-06-28 1985-06-19 Method for the separation of water obtained form a coking process into a small high salt content fraction and a large low salt content fraction

Country Status (6)

Country Link
US (1) US4710302A (en)
EP (1) EP0221061B1 (en)
JP (1) JPS61502540A (en)
KR (1) KR900005099B1 (en)
DE (2) DE3423798A1 (en)
WO (1) WO1986000332A1 (en)

Families Citing this family (16)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE3615132A1 (en) * 1986-05-03 1987-11-05 Bergwerksverband Gmbh METHOD FOR DEBOLISHING A CONCENTRATE OF A REVERSE OSMOSIS SYSTEM IN A COOKERY
EP0272465B1 (en) * 1986-12-10 1993-02-24 BBC Brown Boveri AG Process and device for the separation and/or reaction of particles
EP0274037A1 (en) * 1986-12-10 1988-07-13 BBC Brown Boveri AG Process and device for the separation of particles
DE3926575A1 (en) * 1989-08-11 1991-02-14 Metallgesellschaft Ag PROCESS FOR CLEANING RAW FUEL GAS FROM THE GASIFICATION OF SOLID FUELS
DE4012146A1 (en) * 1990-04-14 1991-10-17 Still Otto Gmbh Precooling of coke-oven gas - with electrostatic filtration and naphthalene scrubbing
DE4012143A1 (en) * 1990-04-14 1991-11-07 Still Otto Gmbh Washing ammonia out of coke oven gas with water - comprises two=stage process without need for distn. of regeneration plant and without environmental and cost drawbacks
DE4012144C1 (en) * 1990-04-14 1991-07-25 Still Otto Gmbh, 4630 Bochum, De Overflow water treatment from coking plants - uses reverse osmosis plant and is carried out without removal of ammonia
DE4012145A1 (en) * 1990-04-14 1991-10-17 Still Otto Gmbh Multistage precooling of coke-oven gas - with naphthalene removal by scrubbing with tar
DE4012141A1 (en) * 1990-04-14 1991-10-17 Still Otto Gmbh METHOD FOR PRE-COOKING RAW COOKING GAS AND FOR DESORPING WASHING WATER AND CONDENSATE OF COOKING
DE4116576C2 (en) * 1991-05-21 1993-12-23 Still Otto Gmbh Process for extracting excess coke oven water as a reverse osmosis permeate
DE4235893C2 (en) * 1992-10-23 2000-07-13 Siemens Ag Process and device for cleaning dusty, hot, flammable gas
DE10007503B4 (en) * 2000-02-18 2004-05-27 Deutsche Montan Technologie Gmbh Process for the treatment of raw coke oven gas
DE10011531A1 (en) * 2000-03-13 2001-09-27 Montan Tech Gmbh Raw coke gas sampler feeds analysis instrument via heated electro-filter protected from condensation via a gas cooler
DE10139172C1 (en) * 2001-08-15 2003-02-06 Montan Tech Gmbh Rinsing pre-coolers of coking plant involves using liquid phase produced from collecting main which has not been impinged with pre-cooler condensate
CN103013583B (en) * 2012-12-05 2014-05-21 浙江大学 Process for dust removing, cooling and tar oil recovering of pyrolysis coal gas
CN105018157B (en) * 2015-08-03 2017-09-19 中冶焦耐工程技术有限公司 A kind of combined type primary cooler

Family Cites Families (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US1747616A (en) * 1922-08-02 1930-02-18 Koppers Co Inc Ammonia-recovery process
DE2542055C3 (en) * 1975-09-20 1985-08-22 Metallgesellschaft Ag, 6000 Frankfurt Process for the treatment of a raw gas from the pressurized gasification of coal
DE2853989C2 (en) * 1978-12-14 1980-07-31 Metallgesellschaft Ag, 6000 Frankfurt Process for the treatment of water-containing condensate from the cooling of the raw gas of the pressurized gasification
FR2496685A1 (en) * 1980-10-13 1982-06-25 Pillard Chauffage PROCESS AND INSTALLATION FOR PRODUCING COLD AND CLEAN COMBUSTIBLE GAS USING A SOLID FUEL GASIFIER
DE3043329C2 (en) * 1980-11-17 1986-12-18 Carl Still Gmbh & Co Kg, 4350 Recklinghausen Process and system for cooling and separating chlorides and fluorides from gas mixtures
US4382866A (en) * 1980-12-09 1983-05-10 Johnson Dennis E J Electro-chemical system for liquid filtration
US4370236A (en) * 1980-12-16 1983-01-25 Phillips Petroleum Company Purification of hydrocarbon streams
US4416754A (en) * 1981-08-24 1983-11-22 Exxon Research And Engineering Co. Compositions and process for dedusting solids-containing hydrocarbon oils

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See references of WO8600332A1 *

Also Published As

Publication number Publication date
DE3423798A1 (en) 1986-01-09
JPH041793B2 (en) 1992-01-14
US4710302A (en) 1987-12-01
KR900005099B1 (en) 1990-07-19
KR860700134A (en) 1986-03-31
WO1986000332A1 (en) 1986-01-16
EP0221061B1 (en) 1988-10-12
DE3565554D1 (en) 1988-11-17
DE3423798C2 (en) 1988-12-01
JPS61502540A (en) 1986-11-06

Similar Documents

Publication Publication Date Title
EP0221061A1 (en) Method for the separation of water obtained form a coking process into a small high salt content fraction and a large low salt content fraction.
EP0095144B1 (en) Treatment of condensates from gases
DE1768652B2 (en) Process for the recovery of ethylene and acetylene from cracked gases
DE1592324A1 (en) Process for cleaning a gas consisting mainly of ammonia
WO1989007636A1 (en) Process for treating coal pyrolysis effluent
DE2619805A1 (en) PROCESS FOR REDUCING THE BIOLOGICAL OXYGEN REQUIREMENT OF GAS CONDENSATE
DE10051349B4 (en) Process and apparatus for recovering naphthalene from raw coke oven gas
DE3614851A1 (en) METHOD FOR COOLING RAW GAS
EP0304427B1 (en) Process for dephenolating waste water from coking plants
DE4012145A1 (en) Multistage precooling of coke-oven gas - with naphthalene removal by scrubbing with tar
DE2517310A1 (en) PROCESS FOR THE REGENERATION OF AQUATIC UREA SOLUTIONS
DE856034C (en) Process for working up the gas-steam mixture driven off from the regeneration stage for alkali carbonate-bicarbonate washing solution
EP1419221B1 (en) Method for scavenging precoolers of a coking plant
DE10007503B4 (en) Process for the treatment of raw coke oven gas
DE617355C (en) Process for removing and recovering oils from distillation gases
DE4012141A1 (en) METHOD FOR PRE-COOKING RAW COOKING GAS AND FOR DESORPING WASHING WATER AND CONDENSATE OF COOKING
DE4012146A1 (en) Precooling of coke-oven gas - with electrostatic filtration and naphthalene scrubbing
DE814632C (en) Process for purifying coke oven gases
DE727557C (en) Process for the production of pyridine bases from gas water
DE971319C (en) Process for the processing of water containing phenols, hydrogen sulphide, carbon dioxide, ammonia and possibly other organic and inorganic substances
DE481306C (en) Process for the recovery of waste water
DE704530C (en) Process for the production of phenols from oils and waste water
DE972725C (en) Process for the purification of coal distillation gases, which are compressed after cooling and then cooled again
DE944987C (en) Process for the removal and recovery of tar, ammonia and ammonia water from gases of dry distillation
DE1671346C (en) Method of using the distillation gas from coking ovens

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

17P Request for examination filed

Effective date: 19861008

AK Designated contracting states

Kind code of ref document: A1

Designated state(s): BE DE FR GB IT NL SE

17Q First examination report despatched

Effective date: 19880229

ITF It: translation for a ep patent filed

Owner name: FIAMMENGHI - DOMENIGHETTI

GRAA (expected) grant

Free format text: ORIGINAL CODE: 0009210

AK Designated contracting states

Kind code of ref document: B1

Designated state(s): BE DE FR GB IT NL SE

GBT Gb: translation of ep patent filed (gb section 77(6)(a)/1977)
REF Corresponds to:

Ref document number: 3565554

Country of ref document: DE

Date of ref document: 19881117

ET Fr: translation filed
PLBE No opposition filed within time limit

Free format text: ORIGINAL CODE: 0009261

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: NO OPPOSITION FILED WITHIN TIME LIMIT

26N No opposition filed
ITTA It: last paid annual fee
EAL Se: european patent in force in sweden

Ref document number: 85902990.2

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: FR

Payment date: 19980508

Year of fee payment: 14

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: SE

Payment date: 19980518

Year of fee payment: 14

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: GB

Payment date: 19980522

Year of fee payment: 14

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: NL

Payment date: 19980527

Year of fee payment: 14

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: BE

Payment date: 19980604

Year of fee payment: 14

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: GB

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 19990619

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: SE

Free format text: THE PATENT HAS BEEN ANNULLED BY A DECISION OF A NATIONAL AUTHORITY

Effective date: 19990629

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: FR

Free format text: THE PATENT HAS BEEN ANNULLED BY A DECISION OF A NATIONAL AUTHORITY

Effective date: 19990630

Ref country code: BE

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 19990630

BERE Be: lapsed

Owner name: BERGWERKSVERBAND G.M.B.H.

Effective date: 19990630

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: NL

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20000101

GBPC Gb: european patent ceased through non-payment of renewal fee

Effective date: 19990619

EUG Se: european patent has lapsed

Ref document number: 85902990.2

NLV4 Nl: lapsed or anulled due to non-payment of the annual fee

Effective date: 20000101

REG Reference to a national code

Ref country code: FR

Ref legal event code: ST

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: DE

Payment date: 20010523

Year of fee payment: 17

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: DE

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20030101