EP0486628A1 - Verfahren zur vorkühlung von kokereirohgas und zur desorption von waschwässern und kondensaten der kokerei - Google Patents
Verfahren zur vorkühlung von kokereirohgas und zur desorption von waschwässern und kondensaten der kokereiInfo
- Publication number
- EP0486628A1 EP0486628A1 EP19910907894 EP91907894A EP0486628A1 EP 0486628 A1 EP0486628 A1 EP 0486628A1 EP 19910907894 EP19910907894 EP 19910907894 EP 91907894 A EP91907894 A EP 91907894A EP 0486628 A1 EP0486628 A1 EP 0486628A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- water
- cooling
- gas
- desorbed
- condensates
- 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.)
- Withdrawn
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
- C10K1/04—Purifying combustible gases containing carbon monoxide by cooling to condense non-gaseous materials
Definitions
- the invention relates to a method for the pre-cooling of raw gas and for the desorption of water, i. H. Washing water and condensate from the coking plant with the help of hot raw coke oven gas.
- the concentration of the hot raw gas of water-soluble gases such as ammonia, hydrogen sulfide and carbon dioxide between the pre-cooling and pre-cooling is influenced to a large extent by the manner in which the water evaporated in the pre-cooling from the area of pre-cooling back into the receiver circuit to be led back.
- the excess water from the coal moisture and the chemical conversion is removed from the receiver circuit in order to be able to remove the fixed salts separated out in the receiver from this area.
- these fixed salts are enriched in the receiver circuit and the excess water is obtained as condensate from the pre-cooling (cf. DE 34 23 798 C2).
- the loss of evaporation from the sprinkler supply must be replenished with condensates from the precooling.
- the gas condensates are collected from a plurality of series-connected, indirectly working pre-coolers, in which the gas is conducted in the usual way in direct current with its condensates, ie gas inlet at the top, gas outlet at the bottom, and placed on the first precooler. so that part of the ingredients absorbed in the colder area is desorbed by the warm gas when it is heated up. The sequence of the first cooler is then added to the template sprinkling circuit.
- wash water from ammonia or hydrogen sulfide washing is introduced in the area of the hot raw gas for desorption, this is done according to the prior art by inserting it into the template sprinkling circuit or directly into the template for immediate gas cooling sprinkler water to be fed in, in order to cause extensive evaporation of the dissolved ingredients.
- the soluble gases such as ammonia, carbon dioxide, etc. hot raw gas and the liquid phase. If, however, the loaded wash water from the hydrogen sulfide or ammonia wash is desorbed here, these ingredients take part in the equilibrium and remain, to a considerable extent, dissolved in the wash water in accordance with the distribution laws between gas and water.
- the precooling of the raw gas cooled directly to approximately water vapor saturation temperature is preferably carried out completely, but at least up to above the naphthalene dew point between approximately 30 and 50 ° C., in countercurrent to the condensates that form, ie. H. with gas flow from bottom to top, and according to feature b), the water to be desorbed is exchanged with the raw gas in countercurrent at any point between the initial charge and the outlet.
- the water to be returned to the original can be condensates from the pre-cooling and / or by counter-current desorbed wash water, which, for. B. were given according to claim 3 in the area of pre-cooling in the raw gas.
- the gas cooled in the receiver up to water vapor saturation is thus cooled further in a countercurrent cooling, i.e. gas inlet below, gas outlet above, and the water loss in the receiver circuit is supplemented with water, i.e. condensates and / or loaded washing water, from this pre-cooling, which when flowing off in the Counterflow to the hot raw gas beforehand have been heated and largely desorbed.
- a countercurrent cooling i.e. gas inlet below, gas outlet above
- water loss in the receiver circuit is supplemented with water, i.e. condensates and / or loaded washing water, from this pre-cooling, which when flowing off in the Counterflow to the hot raw gas beforehand have been heated and largely desorbed.
- the hot raw gas is cooled by the washing water and condensate flowing down in the pre-cooling, while at the same time the washing water and condensate itself are heated and the dissolved volatile constituents corresponding to their heating release the raw gas.
- the water is sprayed into the area of the precooler, in particular with special nozzles, under increased pressure.
- the measure leads to an improved desorption of the water.
- a substance exchanger can be connected in the gas path before the precooling, to which the water that flows from the precooling or, in the case of direct cooling, the water to be discharged from the precooler circuit is added.
- a substance exchanger can be switched into the gas path between the receiver and pre-cooling, to which the loaded washing water to be desorbed is added.
- the condensate of the pre-cooling is additionally brought onto this material exchanger. This has the advantage that the water to be returned to the receiver circuit is previously desorbed by the hot raw gas.
- sorbed gases are introduced into the hot raw gas with the water to be returned to the receiver, so that the hot raw gas brings only very slightly increased concentrations of soluble gases with it.
- desorbed water is desorbed, the lowest possible loading of the desorbed water can be achieved. This concerns above all the ammonia, which is still to a considerable extent soluble in the hot condensate or circulating water even at higher temperatures, while the proportion of carbon dioxide in the hot raw gas is only increased insignificantly even when loaded waters are returned to the receiver circuit and also the hydrogen sulfide and cyanide content do not increase to the extent that is the case with ammonia.
- a mass transfer in the area of the hot raw gas and the pre-cooling can be very severely hindered by the tar contained in the gas and there is a risk that a mass exchanger clogs up
- a separating device preferably an electrofiler to switch into the gas path between the receiver and the material exchanger or pre-cooling. This also gives a desorbed water that is not or only very slightly loaded with tar or solid components.
- the procedure according to claim 10 is particularly suitable for systems with direct pre-cooling, in which the loaded washing water is fed into the circuit cooling water at the head of the cooler and from the circuit water running off at the foot of the direct cooler together with the pre-cooler condensate hot and largely, but still far from being desorbed to equilibrium. If this water is now fed into the primary sprinkling water, further desorption is achieved. If an electrostatic precipitator is not connected between the receiver and the pre-cooling, the effect of a separation from the tar separated in the pre-cooling results.
- Nm 3 a naphthalene content of 3.5 g / Nm3 and an ammonia and hydrogen sulfide content of 7 g / Nm each via lines (5) and (6) in the electrostatic filter (7), while the non-evaporated circuit water and condensed tar run off via lines (5) and (8) into the tar separator (3).
- the non-gaseous constituents such as tar and water drops are separated off in the electrostatic filter (7).
- the tar-water mixture running off the electrostatic filter (7) reaches the tar separator (3) via line (9).
- the gas is now fed via line (10) into the material exchanger (11) and then via line (12) from below into the first precooler (13), in which it is indirectly cooled to 50 ° C. by countercurrent cooling water.
- Via line (14) it gets into the naphthalene washer (15) and from there via line (16) from below into the second precooler (17), in which it flows indirectly through cooling water in countercurrent and directly by feeding 100 m 3 of washing water via line (30), which with u. a. 10 g / 1 ammonia and 1.5 g / 1 hydrogen sulfide is loaded, is cooled to 23 ° C, and this via line
- the water running off has an ammonia content of 4 g / 1 and a hydrogen sulfide content of 0.8 g / 1. It is placed on the head of the mass exchanger (11) via the line (20). Here the ammonia content is reduced to a value of 0.9 g / 1 and the hydrogen sulfide content to 0.2 g / 1.
- the water runs out of the material exchanger (11) via the line (21) and is divided into two partial streams. 23.2 m are fed back into the tar separator via line (22) in order to supplement the evaporation losses of the original circuit water. Via line (23), 125 m of weakly contaminated excess water and desorbed wash water are removed and can be returned to the gas scrubber or removed for excess water purification. To remove the fixed salts, 2 m of template circulation solution are removed from the system per line (24).
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)
- Industrial Gases (AREA)
Description
Claims
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE4012141 | 1990-04-14 | ||
DE19904012141 DE4012141A1 (de) | 1990-04-14 | 1990-04-14 | Verfahren zur vorkuehlung von kokereirohgas und zur desorption von waschwaessern und kondensaten der kokerei |
Publications (1)
Publication Number | Publication Date |
---|---|
EP0486628A1 true EP0486628A1 (de) | 1992-05-27 |
Family
ID=6404460
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP19910907894 Withdrawn EP0486628A1 (de) | 1990-04-14 | 1991-04-15 | Verfahren zur vorkühlung von kokereirohgas und zur desorption von waschwässern und kondensaten der kokerei |
Country Status (3)
Country | Link |
---|---|
EP (1) | EP0486628A1 (de) |
DE (1) | DE4012141A1 (de) |
WO (1) | WO1991016406A1 (de) |
Families Citing this family (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE10051349B4 (de) * | 2000-10-17 | 2005-02-03 | Deutsche Montan Technologie Gmbh | Verfahren und Vorrichtungen zur Gewinnung von Naphtalin aus Koksofenrohgas |
DE10139172C1 (de) * | 2001-08-15 | 2003-02-06 | Montan Tech Gmbh | Verfahren zur Spülung von Vorkühlern einer Kokerei |
DE102014221952A1 (de) * | 2014-10-28 | 2016-04-28 | Thyssenkrupp Ag | Reduzierung von Naphthalin in Kokereigas |
CN109357565A (zh) * | 2018-12-21 | 2019-02-19 | 天脊煤化工集团股份有限公司 | 一种低温甲醇洗原料气预冷却器清洗装置及工艺 |
Family Cites Families (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US1747616A (en) * | 1922-08-02 | 1930-02-18 | Koppers Co Inc | Ammonia-recovery process |
DE959125C (de) * | 1949-09-14 | 1957-02-28 | Elfriede Ella Baehr Geb Schnad | Verfahren zur Gewinnung von Schwefel und Ammoniak aus heissen Gasen |
DE916408C (de) * | 1952-04-02 | 1954-08-09 | F J Collin Ag Zur Verwertung V | Verfahren zur Ammoniakgewinnung aus Kohlendestillationsgasen u. dgl. |
US3451896A (en) * | 1967-04-07 | 1969-06-24 | Otto Construction Corp | Method of cleaning a stream of coke oven gas and apparatus therefor |
DE2209075B2 (de) * | 1972-02-25 | 1974-07-18 | John J. Mckeesport Pa. Kelmar (V.St.A.) | Verschmutzungsfreies Verkokungsverfahren mit Trockenkokskühlung und Anlage zu dessen Durchführung |
DE3423798A1 (de) * | 1984-06-28 | 1986-01-09 | Bergwerksverband Gmbh, 4300 Essen | Verfahren zur auftrennung des beim verkokungsprozess anfallenden wassers in eine kleine salzreiche und eine grosse salzarme fraktion |
-
1990
- 1990-04-14 DE DE19904012141 patent/DE4012141A1/de not_active Ceased
-
1991
- 1991-04-15 WO PCT/DE1991/000309 patent/WO1991016406A1/de not_active Application Discontinuation
- 1991-04-15 EP EP19910907894 patent/EP0486628A1/de not_active Withdrawn
Non-Patent Citations (1)
Title |
---|
See references of WO9116406A1 * |
Also Published As
Publication number | Publication date |
---|---|
DE4012141A1 (de) | 1991-10-17 |
WO1991016406A1 (de) | 1991-10-31 |
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Legal Events
Date | Code | Title | Description |
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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 |
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17P | Request for examination filed |
Effective date: 19920319 |
|
AK | Designated contracting states |
Kind code of ref document: A1 Designated state(s): FR IT NL |
|
17Q | First examination report despatched |
Effective date: 19930202 |
|
RIN1 | Information on inventor provided before grant (corrected) |
Inventor name: POLLERT, GEORG, DR. |
|
RAP1 | Party data changed (applicant data changed or rights of an application transferred) |
Owner name: STILL OTTO GMBH |
|
RAP1 | Party data changed (applicant data changed or rights of an application transferred) |
Owner name: THYSSEN STILL OTTO ANLAGENTECHNIK GMBH |
|
STAA | Information on the status of an ep patent application or granted ep patent |
Free format text: STATUS: THE APPLICATION IS DEEMED TO BE WITHDRAWN |
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18D | Application deemed to be withdrawn |
Effective date: 19941101 |